CN111450561B - 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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- CN111450561B CN111450561B CN202010297307.8A CN202010297307A CN111450561B CN 111450561 B CN111450561 B CN 111450561B CN 202010297307 A CN202010297307 A CN 202010297307A CN 111450561 B CN111450561 B CN 111450561B
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- 239000012159 carrier gas Substances 0.000 title claims abstract description 223
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 106
- 238000000926 separation method Methods 0.000 claims abstract description 98
- 239000002994 raw material Substances 0.000 claims abstract description 70
- 239000000945 filler Substances 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 80
- 238000009835 boiling Methods 0.000 claims description 48
- 239000000047 product Substances 0.000 claims description 44
- 238000010992 reflux Methods 0.000 claims description 29
- 230000000630 rising effect Effects 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000013589 supplement Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 17
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000000605 extraction Methods 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 2
- 230000001502 supplementing effect Effects 0.000 description 3
- 239000000084 colloidal system Substances 0.000 description 2
- 238000005516 engineering process 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
- 239000002245 particle Substances 0.000 description 2
- 239000007787 solid Substances 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
- 238000010586 diagram Methods 0.000 description 1
- 230000008543 heat sensitivity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- 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
- B01D3/10—Vacuum distillation
-
- 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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention belongs to the technical field of extraction and separation, and relates to an energy-saving carrier gas stripping system and a stripping process, wherein the 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 circulation heat exchanger; the top in the gas stripping tower is provided with a heat exchange mass transfer section, and the gas stripping tower, the gas circulation heat exchanger and the heat exchange mass transfer section are sequentially communicated through pipelines; the gas circulation heat exchanger, the separation tank and the stripping tower are sequentially communicated through pipelines; the raw material heater is communicated with the stripping tower; the heat exchange mass transfer section, the carrier gas heater and the stripping tower are sequentially communicated through pipelines; the heat exchange mass transfer section comprises heat exchange tubes and filler, and the heat exchange tubes are tube type heat exchange tubes or coil type heat exchange tubes. The invention has low separation temperature, adopts different carrier gas heating modes for heat exchange and mass transfer, realizes the enrichment and separation of one or more substances through stripping and rectifying, has good separation effect, recycles the heat of the system, reduces the heat consumption and the cold consumption of separation, and saves the energy consumption by 30-50%.
Description
Technical Field
The invention belongs to the technical field of extraction 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 medium of some high-boiling medium, the separation can not be completed by adopting conventional rectification; separating a part of thermosensitive media, a solid particle-containing system and a colloid system, wherein the traditional technology can not separate the thermosensitive media, the solid particle-containing system and the colloid system; the medium separation has the problems of high separation temperature, high medium viscosity, poor separation effect of the traditional separation technology, poor fractionation precision by adopting molecular rectification, short-range rectification, film rectification and the like, high input energy consumption, large occupied area, high operation and maintenance cost and the like.
Disclosure of Invention
Aiming at the technical problems of high separation temperature, poor fractionation precision and high energy consumption in the existing stripping separation, the invention provides an energy-saving carrier gas stripping system and a stripping process.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
An energy-saving carrier gas stripping system comprises a stripping tower, a separating 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 gas stripping tower;
The gas stripping tower, the gas circulation heat exchanger and the separation tank are sequentially connected through pipelines; the gas circulation heat exchanger is connected with the heat exchange mass transfer section through a pipeline; the separating tank is connected with the stripping tower through a pipeline; the raw material heater is connected with the stripping tower through a pipeline; and the heat exchange mass transfer section is connected with the carrier gas heater and the stripping tower in sequence through pipelines.
Further, the gas stripping tower is provided with a raw material inlet, a light component reflux inlet, a carrier gas inlet, a light component outlet, a carrier gas circulation inlet and a heavy component discharge port; the carrier gas inlet and the carrier gas outlet are both arranged on the heat and mass transfer section;
The separating tank is provided with a separating tank inlet, a separating tank top outlet and a separating 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 circulation inlet through pipelines; 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; the bottom outlet of the separating tank is connected with the light component reflux inlet through a pipeline; the gas inlet of the heat exchanger is connected with the outlet at the top of the separation tank through a pipeline.
Further, a first valve is arranged on a pipeline between the bottom outlet of the separating tank and the light component backflow inlet.
Further, the heat exchange mass transfer section comprises heat exchange tubes and filler, wherein the heat exchange tubes are tube type heat exchange tubes or coil type heat exchange tubes; the filler is arranged inside or outside the heat exchange tube.
Furthermore, the separation tank is also provided with a separation tank light component reflux port connected with the outlet at the bottom of the separation tank, and a second valve is also arranged on a pipeline between the outlet at the bottom of the separation tank and the separation tank light component reflux port.
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 materials are preheated and subjected to mass transfer by hot carrier gas, heavy components in the raw materials are discharged; the light component is rectified and separated along with the carrier gas by a heat exchange mass transfer section, and the separated condensed component is extracted as a product; the uncondensed and reduced temperature light components and carrier gas are discharged;
2) The discharged carrier gas and the 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; the condensate is further cooled and separated to obtain a low-boiling product and carrier gas, and the low-boiling product is extracted or partially recycled; 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 2) carrying out heat exchange and mass transfer on the cooling carrier gas sent to the heat exchange and mass transfer in the step 2), and after carrying out heat exchange and mass transfer on the cooling carrier gas and the light components in the step 1), recovering part of heat by the cooling carrier gas, and carrying out mass transfer on the cooling carrier gas and the raw materials after supplementing heat.
Further, the specific implementation process of the step 1) is that the raw materials are heated by a raw material heater and then enter a gas stripping tower, hot light components rise after gas stripping mass transfer, and heavy component drops are discharged from a heavy component discharge port through a pump; when the hot light components rise to the top of the gas stripping tower, heat exchange is carried out between the hot light components and cooling carrier gas of the heat exchange mass transfer section, the hot light components are cooled and are condensed and refluxed by themselves, and the obtained medium-boiling product is extracted from the middle part of the gas stripping tower, so that purification, rectification and separation are realized; the light component and carrier gas whose temperature 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 which come out from the light component outlet enter the gas circulation heat exchanger from the inlet at the top of the heat exchanger to exchange heat and cool to obtain cooling carrier gas and condensate, the cooling carrier gas comes out from the gas outlet of the heat exchanger and returns to the top of the stripping tower through the carrier gas inlet to exchange heat and cool with the light component flowing upwards, the temperature of the light component at the top of the stripping tower is reduced, and meanwhile, a medium-boiling product is obtained;
The condensate flows out from the outlet of the bottom of the heat exchanger, and enters the separating tank from the inlet of the separating tank to be cooled and separated to obtain a low-boiling product and a small part of carrier gas; the small part of carrier gas is returned to the top of the stripping tower after being subjected to heat exchange and cooling in the gas circulation heat exchanger, and the medium-boiling product is obtained while the temperature of the light components flowing out of the top of the stripping tower is reduced; the low-boiling product is directly recovered after coming out of the bottom outlet of the separation tank, or is returned to the light component reflux inlet through a first valve; or returned to the light component reflux mouth of the separation tank through a second valve.
Further, the specific implementation process of the step 3) is that the cooling carrier gas returns to the heat and mass transfer section in the stripping tower from the carrier gas inlet, the cooling carrier gas exchanges heat with the carrier gas and the light components which continuously rise in the stripping tower, and the cooling carrier gas takes away part of heat; and after the cooling carrier gas taking away heat is subjected to heat supplement by the carrier gas heater, the cooling carrier gas returns to the bottom of the stripping tower to carry out mass transfer with the raw materials entering the stripping tower.
The beneficial effects of the invention are as follows:
1. According to the invention, waste heat carried out by the top of the gas stripping tower is recovered through the heat exchange mass transfer section arranged in the gas stripping tower, so that the heat of light components at the top of the gas stripping tower is reduced, the separation temperature is 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 substances through stripping and rectifying, and realizes the enrichment and separation of different substances; meanwhile, the temperature of the light components at the top of the gas stripping tower is reduced through the heat exchange tube, and the heat can be recycled, so that the energy consumption of 30-50 can be saved, and the aim of saving energy is fulfilled.
3. In the invention, the bubble point of the separated substances is reduced by the combined action of the carrier gas and the negative pressure, so that the substances can be distilled at a temperature lower than the normal bubble point to realize separation, and the requirements on the grade of the consumed heat can be 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, the two heat transfer modes and the heat exchange mode are simple in process operation and maintenance, the equipment occupies small space, and the gas stripping tower is suitable for separating substances with high boiling point, heat sensitivity and easy oxidation, and is more suitable for various procedures such as extraction, recovery and the like in the food-grade pharmaceutical fine chemical industry.
Drawings
FIG. 1 shows a first carrier gas stripping column separation device provided by the invention;
FIG. 2 is a schematic diagram of a second carrier gas stripping column separation device according to the present invention;
Wherein:
1-a stripping tower; 11-a raw material inlet; 12-a light component reflux inlet; 13—a carrier gas inlet; 14-a light component outlet; 15-a carrier gas outlet; 16—a carrier gas circulation inlet; 17-a heavy component discharge port; 2-a separation tank; 21-separator tank inlet; 22-separation tank top outlet; 23-bottom outlet of separation tank; 24-a light component reflux port of the separation tank; 3-a raw material reciprocating pump; 4, a raw material heater; 5-a carrier gas heater; 6-a gas circulation heat exchanger; 61-heat exchanger top inlet; 62-heat exchanger gas outlet; 63-the bottom outlet of the heat exchanger; 64—a 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 exchange mass transfer section is arranged in the gas stripping tower 1; specifically, a heat exchange mass transfer section is arranged at the top in the stripping tower 1, so that the light components upwards along with the carrier gas pass through the heat exchange mass transfer section to be subjected to heat exchange and cooling, and the temperature of the light components is reduced.
The gas stripping tower 1, the gas circulation heat exchanger 6 and the separation tank 2 are connected in sequence through pipelines; the gas circulation heat exchanger 6 is connected with the heat exchange 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 mass transfer section is connected with the carrier gas heater 5 and the stripping tower 1 in sequence through pipelines.
In this embodiment, the stripping column 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 port 17.
In the embodiment, a heat exchange mass transfer section is arranged at the inner top of the gas stripping tower 1; the heat exchange 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 exchange mass transfer section.
In this embodiment, the separator tank 2 is provided with a separator tank inlet 21, a separator tank top outlet 22 and a separator tank bottom outlet 23; the top of the separation tank 2 is also provided with a circulating water inlet 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 connected with the carrier gas heater 5 and the carrier gas circulation inlet 16 in sequence through pipelines; the light component outlet 14 is connected with the top inlet 61 of the heat exchanger, the gas outlet 62 of the heat exchanger and the carrier gas inlet 13 in sequence through pipelines; the heavy component discharge port 17 is connected with a discharge pipeline; the light component outlet 14 is connected with the top inlet 61 of the heat exchanger, the bottom outlet 63 of the heat exchanger and the inlet 21 of the separating tank in sequence through pipelines; the bottom outlet 23 of the separating tank is connected with the light component reflux inlet 12 through a pipeline; the heat exchanger gas inlet 64 is connected by piping to the separator tank top outlet 22. The bottom outlet 23 of the separation tank is connected to the light fraction return inlet 12 by a pipe and a first valve is provided on the pipe.
In this embodiment, the carrier gas heater 5 is a direct heater.
Referring to fig. 1, the embodiment further comprises a vacuum pump 8 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 and 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 materials are preheated and subjected to mass transfer by hot carrier gas, heavy components in the raw materials are discharged; the light component is rectified and separated along with the carrier gas by a heat exchange mass transfer section, and the separated condensed component is extracted as a product; the uncondensed and reduced temperature light components and carrier gas are discharged;
2) The discharged carrier gas and the 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; the condensate is further cooled and separated to obtain a low-boiling product and carrier gas, and the low-boiling product is extracted or partially recycled; 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 2) carrying out heat exchange and mass transfer on the cooling carrier gas sent to the heat exchange and mass transfer in the step 2), and after carrying out heat exchange and mass transfer on the cooling carrier gas and the light components in the step 1), recovering part of heat by the cooling carrier gas, and carrying out mass transfer on the cooling carrier gas and the raw materials after supplementing heat.
In this embodiment, the top of the separator tank 2 is vacuum supplied 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 the liquid can be carried out in any mode, so that the bubble point of the separated substance is reduced, the bubble point is 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 reciprocating pump 3 is utilized to carry out stripping after the raw material is heated by the raw material heater 4 and enters the stripping tower 1 from the raw material inlet 11; because the raw materials are transferred with hot carrier gas in the stripping tower 1 from the lower part upwards, heavy components in the raw materials are discharged from a heavy component discharge port 17 through a reciprocating pump; the hot light component in the raw material continuously rises along with the carrier gas and is cooled by the heat exchange of a tube type heat exchange tube at the top of the gas stripping tower 1, the hot light component is cooled, and is condensed and refluxed by itself, and the condensed component is taken as a medium-boiling component to be extracted from an outlet at the middle part of the side of the gas stripping tower 1, so that purification, rectification and separation are realized; non-condensable components, light components which have not been reduced in temperature, are discharged from the light component outlet 14 at the top of the stripping tower as the carrier gas continuously rises;
2) The non-condensable components 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 is discharged from the heat exchanger gas outlet 62 and returns to the tubular heat exchange tubes at the top of the gas stripping tower 1 through the carrier gas inlet 13, and exchanges heat with the light components flowing upwards through the tubular heat exchange tubes for cooling, so that the temperature of the light components at the top of the gas stripping tower 1 is reduced, and a medium-boiling product is obtained;
The condensate flows out from the bottom outlet 63 of the heat exchanger and enters the separation tank 2 from the inlet 21 of the separation tank, and the condensate is further cooled and separated by circulating water to obtain a low-boiling product and a small part of carrier gas; 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, exchanges heat and cools, then comes out from the heat exchanger gas outlet 62 and returns to the tube type heat exchange tube at the top of the stripping tower 1 through the carrier gas inlet 13, thereby reducing the temperature of light components at the top of the stripping tower 1 and obtaining a medium-boiling product; the low-boiling product is recovered after exiting from the bottom outlet 23 of the separation tank or returned to the light component reflux inlet 12 through a first valve, and when the low-boiling product is implemented, the recovery or reflux can be selected according to the components of the low-boiling product;
3) The cooling carrier gas returns to the heat and mass transfer section in the stripping tower from the carrier gas inlet 13, and exchanges heat with the carrier gas and the light components which continuously rise in the stripping tower, so that the cooling carrier gas takes away part of heat, and the temperature of the rising carrier gas and the light components is reduced; after the cooling carrier gas taking away heat is subjected to heat supplement by the carrier gas heater 5, the cooling carrier gas returns to the bottom of the gas stripping tower to carry out mass transfer with the raw materials entering the gas stripping tower 1, so that the separation of heavy components and light components in the raw materials is realized, the heat consumption and the cold consumption are reduced, and the energy-saving efficiency is 30%; the top of the gas stripping tower is provided with a heat exchange tube and a filler in a heat exchange mass transfer section, so that the light components are rectified and separated, and the separation precision is improved.
In this embodiment, vacuum negative pressure can be pumped through the vacuum pump 8, so that the cooling of the carrier gas in the tubular heat exchange tube arranged at the top of the gas stripping tower 1 is realized, and the temperature of the carrier gas is reduced, so that when the light component rising along with the carrier gas passes through the tubular 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 tubular heat exchange tube strengthens mass transfer, realizes rectification separation, and improves the separation precision of the separated matters.
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 stripping column 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 port 17.
In the embodiment, a heat exchange mass transfer section is arranged at the inner top of the gas stripping tower 1; the heat exchange mass transfer section comprises a heat exchange tube and a filler, wherein 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 separator tank 2 is provided with a separator tank inlet 21, a separator tank top outlet 22, a separator tank bottom outlet 23, and a separator tank light fraction return 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 connected with the carrier gas heater 5 and the carrier gas circulation inlet 16 in sequence through pipelines; the light component outlet 14 is connected with the top inlet 61 of the heat exchanger, the gas outlet 62 of the heat exchanger and the carrier gas inlet 13 in sequence through pipelines; the heavy component discharge port 17 is connected with a discharge pipeline; the light component outlet 14 is connected with the top inlet 61 of the heat exchanger and the bottom outlet 63 of the heat exchanger in sequence through pipelines and is connected with the inlet 21 of the separating tank; the bottom outlet 23 of the separation tank is respectively connected with the light component reflux inlet 12, the light component reflux outlet 24 of the separation tank and the low-boiling product pipeline through pipelines; the heat exchanger gas inlet 64 is connected with the separation tank top outlet 22 through a pipeline, the separation tank bottom outlet 23 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 bottom outlet 23 of the separation tank and the light component reflux port 24 of the separation tank.
In this embodiment, the carrier gas heater 5 is an indirect heater.
Referring to fig. 2, the embodiment further comprises a vacuum pump 8 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 and 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 materials are preheated and subjected to mass transfer by hot carrier gas, heavy components in the raw materials are discharged; the light component is rectified and separated along with the carrier gas by a heat exchange mass transfer section, and the separated condensed component is extracted as a product; the uncondensed and reduced temperature light components and carrier gas are discharged;
2) The discharged carrier gas and the 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; the condensate is further cooled and separated to obtain a low-boiling product and carrier gas, and the low-boiling product is extracted or partially recycled; 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 2) carrying out heat exchange and mass transfer on the cooling carrier gas sent to the heat exchange and mass transfer in the step 2), and after carrying out heat exchange and mass transfer on the cooling carrier gas and the light components in the step 1), recovering part of heat by the cooling carrier gas, and carrying out mass transfer on the cooling carrier gas and the raw materials after supplementing heat.
In this embodiment, the top of the separator tank 2 is vacuum supplied 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 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 reciprocating pump 3 is utilized to carry out stripping after the raw material is heated by the raw material heater 4 and enters the stripping tower 1 from the raw material inlet 11; because the raw materials are transferred with hot carrier gas in the stripping tower 1 from the lower part upwards, heavy components in the raw materials are discharged from a heavy component discharge port 17 through a reciprocating pump; the hot light component in the raw material continuously rises along with the carrier gas and is cooled by the coil pipe type heat exchange tube at the top of the gas stripping tower 1, the hot light component is cooled, and is condensed and refluxed by itself, and the condensed component is taken as a medium-boiling component and is extracted from an outlet at the middle part of the side of the gas stripping tower 1, so that the purification, rectification and separation are realized; non-condensable components, light components which have not been reduced in temperature, are discharged from the light component outlet 14 at the top of the stripping tower as the carrier gas continuously rises;
2) The non-condensable components 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 is discharged from the heat exchanger gas outlet 62 and returns to the coil type heat exchange tube at the top of the stripping tower 1 through the carrier gas inlet 13, and exchanges heat with the light components flowing upwards through the coil type heat exchange tube for cooling, so that the temperature of the light components at the top of the stripping tower 1 is reduced, and a medium-boiling product is obtained;
The condensate flows out from the bottom outlet 63 of the heat exchanger and enters the separation tank 2 from the inlet 21 of the separation tank, and the condensate is further cooled and separated by circulating water to obtain a low-boiling product and a small part of carrier gas; 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, exchanges heat and cools, then comes out from the heat exchanger gas outlet 62 and returns to the coil type heat exchange tube at the top of the stripping tower 1 through the carrier gas inlet 13, thereby reducing the temperature of light components at the top of the stripping tower 1 and obtaining a medium-boiling product; the low-boiling product is recovered after exiting from the bottom outlet 23 of the separation tank, or is returned to the light component reflux inlet 12 through a first valve, or is returned to the light component reflux outlet 24 of the separation tank through a second valve, and when the low-boiling product is implemented, the recovery or reflux can be selected according to the components of the low-boiling product, and the recovery or reflux can be controlled through the first valve and the second valve;
3) The cooling carrier gas returns into a coiled heat exchange tube at the top of the stripping tower from the carrier gas inlet 13, and exchanges heat with the light components in the stripping tower along with the continuous rising of the carrier gas, so that the bubble point temperature of the light components along with the continuous rising of the carrier gas is reduced, stripping separation is realized, meanwhile, the cooling carrier gas carries heat after heat exchange, and after the temperature rise, the cooling carrier gas comes out from the carrier gas outlet 15 and is supplemented with heat by the carrier gas heater 5, finally, the cooling carrier gas enters the bottom of the stripping tower 1 in a circulating way from the carrier gas circulating inlet 16 and is in mass transfer with raw materials entering the stripping tower; therefore, the heat recycling 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%, and the energy saving purpose is realized; the top of the gas stripping tower is provided with a heat exchange tube and a filler in a heat exchange mass transfer section, so that the light components are rectified and separated, and the separation precision is improved.
In this embodiment, the vacuum pump 8 may be used to pump vacuum negative pressure to cool the carrier gas in the coil heat exchange tube at the top of the gas stripping tower 1, so that the temperature of the carrier gas is reduced, and when the light component rising with the carrier gas passes through the coil heat exchange tube at the top of the gas stripping tower 1, the temperature of the light component is reduced to the maximum extent, the packing outside the coil heat exchange tube enhances mass transfer, and the separation precision of the separated material is improved, and meanwhile, the medium boiling product is obtained.
In summary, 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 distilled at a temperature lower than the normal bubble point to realize separation; the integrated heat exchange is realized through the gas stripping tower and the separating tank, the mass transfer is enhanced, and the separation precision of the separated objects is improved; the invention provides two heat exchange modes and heating modes, the separation temperature is low, the separation precision is high, the separated substances are not polluted, the energy consumption is low, the method is suitable for separating high-boiling point, thermosensitive and easily-oxidized substances, and is more suitable for various procedures of extraction, recovery and the like in the food-grade pharmaceutical fine chemical industry.
Claims (8)
1. An energy-saving carrier gas stripping system is characterized in that: the energy-saving carrier gas stripping system comprises a stripping tower (1), a separation tank (2), a raw material heater (4), a carrier gas heater (5) and a gas circulation heat exchanger (6);
A heat exchange mass transfer section is arranged in the gas stripping tower (1); the heat exchange mass transfer section comprises a heat exchange tube and a filler, wherein the heat exchange tube is a tube type heat exchange tube, and the filler is arranged inside or outside the heat exchange tube;
The gas stripping tower (1), the gas circulation heat exchanger (6) and the separation tank (2) are sequentially connected through pipelines; the gas circulation heat exchanger (6) is connected with the heat exchange mass transfer section through a pipeline; the separating 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 mass transfer section is connected with the carrier gas heater (5) and the stripping tower (1) in sequence through pipelines;
The device also comprises a raw material reciprocating pump (3);
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 circulation inlet (16) and a heavy component discharge port (17); the carrier gas inlet (13) and the carrier gas outlet (15) are both arranged on the heat and mass transfer section;
The separating tank (2) is provided with a separating tank inlet (21), a separating tank top outlet (22) and a separating 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 circulation inlet (16) through pipelines; the light component outlet (14) is sequentially connected with the top inlet (61), the gas outlet (62) and the carrier gas inlet (13) of the heat exchanger through pipelines;
The light component outlet (14) is sequentially connected with the top inlet (61), the bottom outlet (63) and the separating tank inlet (21) of the heat exchanger through pipelines; the bottom outlet (23) of the separation tank is connected with the light component reflux inlet (12) through a pipeline; 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 specific separation process is as follows:
1) Heating raw materials by a raw material reciprocating pump (3) through a raw material heater (4), and then feeding the raw materials into a stripping tower (1) from a raw material inlet (11) for stripping; because the raw material is transferred with hot carrier gas in the stripping tower (1) from the lower part upwards, heavy components in the raw material are discharged from a heavy component discharge port (17) through a reciprocating pump; the hot light component in the raw material continuously rises along with the carrier gas and is cooled by the heat exchange of a tube type heat exchange tube at the top of the gas stripping tower (1), the hot light component is cooled and is condensed and reflowed by itself, and the condensed component is taken as a medium-boiling component and is extracted from an outlet at the middle part of the side of the gas stripping tower (1), so that the purification, rectification and separation are realized; the non-condensable components are light components with reduced temperature, and the cooled light components are continuously discharged from a light component outlet (14) at the top of the stripping tower along with the rising of carrier gas;
2) Non-condensable components from the light component outlet (14) enter a gas circulation heat exchanger (6) from a heat exchanger top inlet (61) for heat exchange and cooling to obtain cooling carrier gas and condensate, the cooling carrier gas is discharged from a heat exchanger gas outlet (62) and returns to a tubular heat exchange tube at the top of the stripping tower 1 through a carrier gas inlet (13), and exchanges heat with the light components flowing upwards through the tubular heat exchange tube for cooling, so that the temperature of the light components at the top of the stripping tower 1 is reduced, and a medium-boiling product is obtained;
The condensate flows out from an outlet (63) at the bottom of the heat exchanger, enters a separating tank (2) from an inlet (21) of the separating tank, and is further cooled and separated by circulating water to obtain a low-boiling product and a small part of carrier gas; 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, and then comes out from the gas outlet (62) of the heat exchanger and returns to the tube array type heat exchange tube at the top of the stripping tower (1) through the carrier gas inlet (13), so that the temperature of light components at the top of the stripping tower (1) is reduced, and a medium-boiling product is obtained; the low-boiling product is recovered after exiting from the bottom outlet (23) of the separation tank or returned to the light component reflux inlet (12) through a first valve, and when the low-boiling product is implemented, the recovery or reflux can be selected according to the components of the low-boiling product;
3) The cooling carrier gas returns to the heat and mass transfer section in the stripping tower from the carrier gas inlet (13), and exchanges heat with the carrier gas and the light components which continuously rise in the stripping tower, and the cooling carrier gas takes away part of heat, so that the temperatures of the rising carrier gas and the light components are reduced; after the cooling carrier gas taking away heat is subjected to heat supplement by the carrier gas heater (5), the cooling carrier gas returns to the bottom of the stripping tower to carry out mass transfer with the raw materials entering the stripping tower (1), so that the separation of heavy components and light components in the raw materials is realized, the heat consumption and the cold consumption are reduced, and the energy-saving efficiency is 30%; the top of the gas stripping tower is provided with a heat exchange tube and a filler in a heat exchange mass transfer section, so that the light components are rectified and separated, and the separation precision is improved.
2. The energy-efficient carrier gas stripping system as set forth in claim 1, wherein: a first valve is arranged on a pipeline between the bottom outlet (23) of the separation tank and the light component reflux inlet (12).
3. The energy-efficient carrier gas stripping system as set forth in claim 1, wherein: the separation tank (2) is also provided with a separation tank light component reflux port (24) connected with a separation tank bottom outlet (23), and a second valve is also arranged on a pipeline between the separation tank bottom outlet (23) and the separation tank light component reflux port (24).
4. The energy-efficient carrier gas stripping system as set forth in claim 1, wherein: the carrier gas heater (5) is a direct heater or an indirect heater.
5. A stripping process based on the energy-saving carrier gas stripping system as claimed in any one of claims 1 to 4, characterized in that: the stripping process comprises the following steps:
1) After the raw materials are preheated and subjected to mass transfer by hot carrier gas, heavy components in the raw materials are discharged; the light component is rectified and separated along with the carrier gas by a heat exchange mass transfer section, and the separated condensed component is extracted as a product; the uncondensed and reduced temperature light components and carrier gas are discharged;
2) The discharged carrier gas and the light components are subjected to heat exchange and cooling to obtain cooling carrier gas and condensate, and the cooling carrier gas is sent to a heat exchange mass transfer section; the condensate is further cooled and separated to obtain a low-boiling product and carrier gas, and the low-boiling product is extracted or partially recycled; after the carrier gas is subjected to heat exchange and cooling, the cooled carrier gas is sent to a heat exchange mass transfer section;
3) And 2) carrying out heat exchange and mass transfer on the cooling carrier gas sent to the heat exchange and mass transfer section in the step 2) and the carrier gas and the light component in the step 1), and recovering part of heat by the cooling carrier gas, and carrying out mass transfer on the cooling carrier gas and the raw material after heat compensation.
6. The stripping process as claimed in claim 5, wherein: the specific implementation process of the step 1) is that the raw materials enter a gas stripping tower (1) after being heated by a raw material heater (4), hot light components rise after gas stripping mass transfer, and heavy components fall and are discharged from a heavy component discharge port (17) through a reciprocating pump; when the hot light components rise to the top of the gas stripping tower (1), heat exchange is carried out between the hot light components and cooling carrier gas of the heat exchange mass transfer section, the hot light components are cooled and are condensed and refluxed by themselves, and the obtained medium-boiling product is extracted from the middle part of the gas stripping tower (1), so that purification, rectification and separation are realized; the light component and carrier gas whose temperature is lowered are discharged from the light component outlet (14).
7. The stripping process as claimed in claim 5, wherein: in the step 2), the light components and the carrier gas which come out from the light component outlet (14) enter a gas circulation heat exchanger (6) from a heat exchanger top inlet (61) for heat exchange and cooling to obtain cooling carrier gas and condensate, the cooling carrier gas comes out from a heat exchanger gas outlet (62) and returns to the top of the stripping tower (1) through a carrier gas inlet (13), heat exchange and cooling are carried out on the cooling carrier gas and the light components which flow upwards, the temperature of the light components at the top of the stripping tower (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 a separating tank (2) 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; the small part of carrier gas is returned to the top of the stripping tower (1) after being subjected to heat exchange and cooling in the gas circulation heat exchanger (6), and the medium-boiling product is obtained while the temperature of the light components at the top of the stripping tower (1) is reduced; the low-boiling product is directly recovered after coming out of the bottom outlet (23) of the separation tank, or is returned to the light component reflux inlet (12) through a first valve; or returned to the knock-out pot light component return port (24) through a second valve.
8. The stripping process as claimed in claim 5, wherein: in the step 3), the specific implementation process of the step 3) is that cooling carrier gas returns to a heat exchange mass transfer section in the stripping tower from a carrier gas inlet (13), the cooling carrier gas exchanges heat with the carrier gas and the light components which continuously ascend in the stripping tower, and the cooling carrier gas takes away part of heat; after the cooling carrier gas taking away heat is subjected to heat supplement by the carrier gas heater (5), the cooling carrier gas returns to the bottom of the stripping tower to carry out mass transfer with the raw materials entering the stripping tower (1).
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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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