CN213823507U - Evaporating device and miscella evaporating device in middle of miscella - Google Patents
Evaporating device and miscella evaporating device in middle of miscella Download PDFInfo
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- CN213823507U CN213823507U CN202022623418.1U CN202022623418U CN213823507U CN 213823507 U CN213823507 U CN 213823507U CN 202022623418 U CN202022623418 U CN 202022623418U CN 213823507 U CN213823507 U CN 213823507U
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Abstract
The utility model relates to an intermediate evaporation plant and miscella evaporation plant belongs to grain and oil processing technology field. The utility model discloses research and development is solved that the mist is direct to be condensed through the condenser, and the heat source fails to utilize the problem that causes the energy waste. The system comprises a heat exchanger, a drainage pump, a flash tank and an intermediate pump, wherein the drainage pump is connected with the heat exchanger, the heat exchanger is connected with the flash tank, and the flash tank is connected with the intermediate pump. The waste heat in the mixed gas in the stripping tower and the drying tower is fully utilized, and the energy utilization rate is improved.
Description
Technical Field
The utility model relates to an intermediate evaporation plant and miscella evaporation plant belongs to grain and oil processing technology field.
Background
In the negative pressure evaporation process of the mixed oil squeezed by soybeans, the traditional evaporation process is to perform twice film-lifting evaporation on the mixed oil with the temperature of about 55 ℃ and the concentration of about 38% by three sets of evaporation equipment, namely a first long tube evaporator, a second long tube evaporator and a stripping tower, under the condition that the operating pressure is not lower than 350mbar, improve the concentration of the mixed oil to be not lower than 95%, and finally purify the concentration of the mixed oil to be not lower than 99.5% by utilizing the steam distillation principle through the stripping tower so as to complete the separation of solvent and grease. The production process is completed by heating with fresh steam during the second evaporation, and the steam consumption is high.
The concentration of the mixed oil from the mixed oil tank of the leacher at the present stage is 38 percent, the temperature of the mixed oil at the outlet after the first steaming is finished is 60 ℃, and the concentration of the mixed oil is about 70 percent. The mixed gas from the stripping tower and the crude oil dryer is the mixed gas with the main components of water vapor and n-hexane, the flow rate is 3638kg/h, wherein the water vapor accounts for 2420kg/h, the operating pressure is 350mbar, the temperature is about 98 ℃, the mixed gas is directly condensed by an E126 condenser, and a heat source cannot be utilized.
Therefore, it is desirable to provide an intermediate evaporation device for mixed oil to solve the above technical problems.
SUMMERY OF THE UTILITY MODEL
The utility model discloses research and development is solved that the mist is direct to be condensed through the condenser, and the heat source fails to utilize the problem that causes the energy waste. A brief summary of the present invention is provided below in order to provide a basic understanding of some aspects of the present invention. It should be understood that this summary is not an exhaustive overview of the invention. It is not intended to identify key or critical elements of the invention or to delineate the scope of the invention.
The technical scheme of the utility model:
the utility model provides an evaporation plant in middle of miscella, includes middle heat exchanger, drain pump, flash tank and intermediate pump, and the drain pump is connected with middle heat exchanger, and middle heat exchanger is connected with the flash tank, and the flash tank is connected with the intermediate pump.
Preferably: the lower end of the middle heat exchanger is provided with a middle oil inlet, the lower part of the side wall of the middle heat exchanger is provided with a middle water outlet, the upper part of the side wall of the middle heat exchanger is provided with a heat conduction port, the side wall of the middle heat exchanger is provided with a middle solvent outlet, the middle water outlet is positioned at the lower side of the middle solvent outlet, the side wall of the middle heat exchanger is provided with a middle oil outlet, and the middle water outlet is connected with a drainage pump;
the upper end of the flash tank is provided with a flash solvent outlet, the lower end of the flash tank is provided with a flash oil outlet, the side wall of the flash tank is provided with a flash oil inlet, the middle oil outlet is connected with the flash oil inlet through an oil pipe, and the flash oil outlet is connected with a middle pump.
Preferably: the draining pump is connected with the water dividing tank.
The utility model provides an evaporation plant in middle of miscella, including first evaporimeter, middle evaporation plant, the heat exchanger, the second evaporimeter, the condenser, first oil pump, the strip tower, second oil pump and drying tower, first evaporimeter passes through oil piping connection with middle evaporation plant, middle evaporation plant passes through oil piping connection with the heat exchanger, the heat exchanger is connected with the second evaporimeter, first evaporimeter, middle evaporation plant and second evaporimeter all pass through the condensing agent union coupling with the condenser, the second evaporimeter passes through first oil pump and is connected with the strip tower, the strip tower passes through the second oil pump and is connected with the drying tower, strip tower and drying tower all are connected with middle evaporation plant through the heat pipe.
Preferably: the lower part of the first evaporator is provided with a secondary steam inlet and a first oil outlet, and the upper end of the first evaporator is provided with a first solvent outlet;
the lower end of the second evaporator is provided with a second oil inlet and a second oil outlet, and the upper end of the second evaporator is provided with a second solvent outlet;
the side wall of the stripping tower is provided with a stripping tower oil inlet, the top end of the stripping tower is provided with a stripping tower heat conducting port, and the lower part of the stripping tower is provided with a stripping tower oil outlet;
the side wall of the drying tower is provided with a drying tower oil inlet, the top end of the drying tower is provided with a drying tower heat conducting port, and the lower end of the drying tower is provided with a drying tower oil outlet;
the condenser includes first condenser, second condenser and third condenser, first oil-out is connected with middle oil inlet, first solvent export, flash distillation solvent export and second solvent export all are connected with first condenser and second condenser, drying tower heat conduction mouth, strip tower heat conduction mouth and third condenser are connected to the heat conduction mouth, middle solvent export is connected with the third condenser, the intermediate pump is connected with the heat exchanger, the heat exchanger is connected with the second oil inlet, the second oil-out is connected with strip tower oil inlet through first oil pump, the strip tower oil-out is connected with the drying tower oil inlet through the second oil pump, the drying tower oil-out is connected with the end pump.
The utility model discloses following beneficial effect has:
1. the waste heat in the mixed gas in the stripping tower and the drying tower is fully utilized, and the energy utilization rate is improved;
2. the solvent gas after flash evaporation enters a condenser for condensation, condensate of the vertical tubular heat exchanger W404 is pumped into an E129 water separation tank through a centrifugal pump for solvent water separation, and the system achieves the purpose of saving the use of fresh steam of an evaporation system by recovering waste heat of a stripping tower and a drying tower;
3. the temperature of the mixed oil entering the intermediate heat exchanger through the first evaporator is increased from 60 ℃ to 67 ℃, the concentration of the mixed oil is increased from 70% to 87.8%, 1.55 tons of fresh steam is saved per hour, 6.2 kilograms of steam is saved per ton of beans, the annual startup is carried out according to 300 days, the steam cost of one device is saved by 120 ten thousand yuan per year, and great economic benefit is created.
Drawings
FIG. 1 is a schematic view of a mixed oil evaporating apparatus;
FIG. 2 is a schematic view showing the construction of a mixed oil intermediate evaporation apparatus;
in the figure, 1-a first evaporator, 10-a secondary steam inlet, 11-a first oil outlet, 12-a first solvent outlet, 2-an intermediate evaporation device, 21-an intermediate heat exchanger, 210-an intermediate oil inlet, 211-an intermediate water outlet, 212-an intermediate solvent outlet, 213-a heat conduction port, 214-an intermediate oil outlet, 22-a drainage pump, 23-a flash tank, 231-a flash oil outlet, 232-a flash oil inlet, 233-a flash solvent outlet, 24-an intermediate pump, 3-a heat exchanger, 4-a second evaporator, 41-a second oil inlet, 42-a second solvent outlet, 43-a second oil outlet, 51-a first condenser, 52-a second condenser, 53-a third condenser and 6-a first oil pump, 7-stripping tower, 71-stripping tower oil inlet, 72-stripping tower heat conduction port, 73-stripping tower oil outlet, 8-second oil pump, 9-drying tower, 91-drying tower heat conduction port, 92-drying tower oil inlet, and 93-drying tower oil outlet.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described below with reference to specific embodiments shown in the accompanying drawings. It should be understood that the description is intended to be illustrative only and is not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
The utility model discloses the connection that mentions divide into fixed connection and can dismantle the connection, fixed connection is for the conventional fixed connection mode such as undetachable connection including but not limited to hem connection, rivet connection, adhesive connection and welded connection, can dismantle the connection including but not limited to conventional dismantlement modes such as threaded connection, buckle connection, pin joint and hinged joint, when not clearly prescribing a limit to concrete connection mode, acquiesces to always can find at least one kind of connected mode in current connected mode and can realize this function, and the technical staff in the art can select by oneself as required. For example: the fixed connection selects welding connection, and the detachable connection selects hinge connection.
The first embodiment is as follows: the present embodiment will be described with reference to fig. 2, and the mixed oil intermediate evaporation apparatus of the present embodiment includes an intermediate heat exchanger 21, a drain pump 22, a flash tank 23, and an intermediate pump 24, the drain pump 22 being connected to the intermediate heat exchanger 21, the intermediate heat exchanger 21 being connected to the flash tank 23, and the flash tank 23 being connected to the intermediate pump 24.
The second embodiment is as follows: the embodiment is described with reference to fig. 2, in the mixed oil intermediate evaporation device of the embodiment, the lower end of the intermediate heat exchanger 21 is provided with an intermediate oil inlet 210, the lower part of the side wall of the intermediate heat exchanger 21 is provided with an intermediate water outlet 211, the upper part of the side wall of the intermediate heat exchanger 21 is provided with a heat conduction port 213, the side wall of the intermediate heat exchanger 21 is provided with an intermediate solvent outlet 212, the intermediate water outlet 211 is located at the lower side of the intermediate solvent outlet 212, the side wall of the intermediate heat exchanger 21 is provided with an intermediate oil outlet 214, and the intermediate water outlet 211 is connected with the drainage pump 22;
the upper end of the flash tank 23 is provided with a flash solvent outlet 233, the lower end of the flash tank 23 is provided with a flash oil outlet 231, the side wall of the flash tank 23 is provided with a flash oil inlet 232, the middle oil outlet 214 is connected with the flash oil inlet 232 through an oil pipe, and the flash oil outlet 231 is connected with the middle pump 24.
The third concrete implementation mode: in the present embodiment, the drain pump 22 is connected to the water separation tank, and the mixed oil intermediate evaporation apparatus of the present embodiment will be described with reference to fig. 2.
The fourth concrete implementation mode: the embodiment is described with reference to fig. 1-2, and the mixed oil evaporation device of the embodiment includes a first evaporator 1, an intermediate evaporation device 2, a heat exchanger 3, a second evaporator 4, a condenser, a first oil pump 6, a stripping tower 7, a second oil pump 8 and a drying tower 9, wherein the first evaporator 1 is connected with the intermediate evaporation device 2 through an oil pipe, the intermediate evaporation device 2 is connected with the heat exchanger 3 through an oil pipe, the heat exchanger 3 is connected with the second evaporator 4, the first evaporator 1, the intermediate evaporation device 2 and the second evaporator 4 are all connected with the condenser through a condensing agent pipe, the second evaporator 4 is connected with the stripping tower 7 through the first oil pump 6, the stripping tower 7 is connected with the drying tower 9 through the second oil pump 8, and the stripping tower 7 and the drying tower 9 are all connected with the intermediate evaporation device 2 through a heat conduction pipe;
the intermediate evaporation device 2 comprises a heat exchanger 21, a drainage pump 22, a flash tank 23 and an intermediate pump 24, wherein the drainage pump 22 is connected with the heat exchanger 21, the heat exchanger 21 is connected with the flash tank 23, and the flash tank 23 is connected with the intermediate pump 24;
the lower end of the intermediate heat exchanger 21 is provided with an intermediate oil inlet 210, the lower part of the side wall of the intermediate heat exchanger 21 is provided with an intermediate water outlet 211, the upper part of the side wall of the intermediate heat exchanger 21 is provided with a heat conduction port 213, the side wall of the intermediate heat exchanger 21 is provided with an intermediate solvent outlet 212, the intermediate water outlet 211 is positioned at the lower side of the intermediate solvent outlet 212, the side wall of the intermediate heat exchanger 21 is provided with an intermediate oil outlet 214, and the intermediate water outlet 211 is connected with the drainage pump 22;
the upper end of the flash tank 23 is provided with a flash solvent outlet 233, the lower end of the flash tank 23 is provided with a flash oil outlet 231, the side wall of the flash tank 23 is provided with a flash oil inlet 232, the middle oil outlet 214 is connected with the flash oil inlet 232 through an oil pipe, and the flash oil outlet 231 is connected with the middle pump 24;
the drain pump 22 is connected to the water diversion tank.
The fifth concrete implementation mode: the embodiment is described with reference to fig. 1-2, and the mixed oil intermediate evaporation device of the embodiment has a secondary steam inlet 10 and a first oil outlet 11 at the lower part of a first evaporator 1, and a first solvent outlet 12 at the upper end of the first evaporator 1;
the lower end of the second evaporator 4 is provided with a second oil inlet 41 and a second oil outlet 43, and the upper end of the second evaporator 4 is provided with a second solvent outlet 42;
the side wall of the stripping tower 7 is provided with a stripping tower oil inlet 71, the top end of the stripping tower 7 is provided with a stripping tower heat conducting port 72, and the lower part of the stripping tower 7 is provided with a stripping tower oil outlet 73;
the side wall of the drying tower 9 is provided with a drying tower oil inlet 92, the top end of the drying tower 9 is provided with a drying tower heat conduction port 91, and the lower end of the drying tower 9 is provided with a drying tower oil outlet 93;
the condenser comprises a first condenser 51, a second condenser 52 and a third condenser 53, a first oil outlet 11 is connected with an intermediate oil inlet 210, a first solvent outlet 12, a flash solvent outlet 233 and a second solvent outlet 42 are respectively connected with the first condenser 51 and the second condenser 52, a drying tower heat conduction port 91, a stripping tower heat conduction port 72 and the third condenser 53 are connected to a heat conduction port 213, an intermediate solvent outlet 212 is connected with the third condenser 53, an intermediate pump 24 is connected with a heat exchanger 3, the heat exchanger 3 is connected with a second oil inlet 41, a second oil outlet 43 is connected with a stripping tower oil inlet 71 through a first oil pump 6, a stripping tower oil outlet 73 is connected with a drying tower oil inlet 92 through a second oil pump 8, and a drying tower oil outlet 93 is connected with a tail end pump.
The working principle is as follows: the secondary mixed oil steam enters the first evaporator 1 through the secondary steam inlet 10 for cooling, the condensing agent is still in a gaseous state due to the low boiling point of the condensing agent, and enters the first condenser 51 and the second condenser 52 through the first solvent outlet 12, the liquid mixed oil enters the intermediate heat exchanger 21 through the first oil outlet 11 and the intermediate oil inlet 210, because of different densities, part of the condensing agent sinks at the lower part of the mixed oil to achieve the purpose of separation, the mixed oil enters the flash tank 23 through the intermediate oil outlet 214 and the flash oil inlet 232, the sinking condensing agent enters the third condenser 53 through the intermediate solvent outlet 212, the mixed oil in the flash tank 23 volatilizes during temperature rising and enters the first condenser 51 and the second condenser 52 through the flash solvent outlet 233, the mixed oil enters the heat exchanger 3 through the flash oil outlet 231 under the action of the intermediate pump 24 for heat exchange, and then enters the second evaporator 4 through the second oil inlet 41, after the solvent is evaporated, the solvent enters the first condenser 51 and the second condenser 52 through the second solvent outlet 42, the mixed oil enters the stripping tower 7 through the second oil outlet 43 and the stripping tower oil inlet 71 under the action of the first oil pump 6, and the mixed oil in the stripping tower 7 enters the drying tower 9 through the stripping tower oil outlet 73 and the drying tower oil inlet 92 under the action of the second oil pump 8; the stripping tower 7 and the drying tower 9 are both provided with mixed gas, the mixed gas is the mixed gas with the main components of water vapor and normal hexane, in order to fully utilize the residual heat in the mixed gas in the stripping tower 7 and the drying tower 9, the mixed gas is utilized to exchange heat with the mixed oil in the heat exchanger 21, the tube side medium is the mixed oil, the shell side medium is the mixed gas, the mixed gas in the stripping tower 7 enters the intermediate heat exchanger 21 through the heat conducting port 213, the mixed gas in the drying tower 9 enters the heat exchanger 21 through the heat conducting port 91 of the drying tower, after the two-phase medium fully exchanges heat, the mixed oil enters a flash tank with the operating pressure kept at 350mbar, the mixed oil after flash evaporation enters a second evaporator 4 to be evaporated continuously, the heat exchanger 21 is a vertical type tubular heat exchanger W404, the drainage pump 22 is a centrifugal pump, and the condensing agent of the vertical type tubular heat exchanger W404 is pumped into an E129 water separation tank through the centrifugal pump to carry out solvent water separation. The system achieves the purpose of saving the use of fresh steam of the evaporation system by recovering the waste heat of the stripping tower and the dryer;
and the solvent gas after flash evaporation enters an E116-1-2 condenser for condensation, and the condensate of the vertical tubular heat exchanger W404 is pumped into an E129 water separation box through a centrifugal pump for solvent water separation. The system achieves the purpose of saving the use of fresh steam of the evaporation system by recovering the waste heat of the stripping tower and the dryer; the temperature of the mixed oil entering the intermediate heat exchanger 21 through the first evaporator 1 is increased from 60 ℃ to 67 ℃, the concentration of the mixed oil is increased from 70% to 87.8%, 1.55 tons of fresh steam is saved per hour, 6.2 kilograms of steam is saved per ton of beans, the annual startup is carried out according to 300 days, the steam cost of one device is saved by 120 ten thousand yuan per year, and great economic benefit is created.
It should be noted that, in the above embodiments, as long as the technical solutions can be aligned and combined without contradiction, those skilled in the art can exhaust all possibilities according to the mathematical knowledge of the alignment and combination, and therefore the present invention does not describe the technical solutions after alignment and combination one by one, but it should be understood that the technical solutions after alignment and combination have been disclosed by the present invention.
This embodiment is only illustrative of the patent and does not limit the scope of protection thereof, and those skilled in the art can make modifications to its part without departing from the spirit of the patent.
Claims (4)
1. The utility model provides an evaporation plant in middle of miscella which characterized in that: the system comprises an intermediate heat exchanger (21), a drainage pump (22), a flash tank (23) and an intermediate pump (24), wherein the drainage pump (22) is connected with the intermediate heat exchanger (21), the intermediate heat exchanger (21) is connected with the flash tank (23), and the flash tank (23) is connected with the intermediate pump (24);
the lower end of the intermediate heat exchanger (21) is provided with an intermediate oil inlet (210), the lower part of the side wall of the intermediate heat exchanger (21) is provided with an intermediate water outlet (211), the upper part of the side wall of the intermediate heat exchanger (21) is provided with a heat conduction port (213), the side wall of the intermediate heat exchanger (21) is provided with an intermediate solvent outlet (212), the intermediate water outlet (211) is positioned at the lower side of the intermediate solvent outlet (212), the side wall of the intermediate heat exchanger (21) is provided with an intermediate oil outlet (214), and the intermediate water outlet (211) is connected with a drainage pump (22);
the upper end of the flash tank (23) is provided with a flash solvent outlet (233), the lower end of the flash tank (23) is provided with a flash oil outlet (231), the side wall of the flash tank (23) is provided with a flash oil inlet (232), the middle oil outlet (214) is connected with the flash oil inlet (232) through an oil pipe, and the flash oil outlet (231) is connected with the middle pump (24).
2. The intermediate evaporation device for mixed oil according to claim 1, wherein: the drainage pump (22) is connected with the water diversion box.
3. The utility model provides a miscella evaporation plant which characterized in that: comprises a first evaporator (1), an intermediate evaporation device (2), a heat exchanger (3), a second evaporator (4), a condenser, a first oil pump (6), a stripping tower (7), a second oil pump (8) and a drying tower (9), wherein the first evaporator (1) is connected with the intermediate evaporation device (2) through an oil pipe, the intermediate evaporation device (2) is connected with the heat exchanger (3) through an oil pipe, the heat exchanger (3) is connected with the second evaporator (4), the first evaporator (1), the intermediate evaporation device (2) and the second evaporator (4) are all connected with the condenser through condensing agent pipes, the second evaporator (4) is connected with the stripping tower (7) through the first oil pump (6), the stripping tower (7) is connected with the drying tower (9) through the second oil pump (8), the stripping tower (7) and the drying tower (9) are both connected with the intermediate evaporation device (2) through heat conducting pipes, the intermediate evaporation device (2) adopts a mixed oil intermediate evaporation device as claimed in any one of claims 1-2.
4. A mixed oil evaporating unit as set forth in claim 3, wherein: the lower part of the first evaporator (1) is provided with a secondary steam inlet (10) and a first oil outlet (11), and the upper end of the first evaporator (1) is provided with a first solvent outlet (12);
the lower end of the second evaporator (4) is provided with a second oil inlet (41) and a second oil outlet (43), and the upper end of the second evaporator (4) is provided with a second solvent outlet (42);
the side wall of the stripping tower (7) is provided with a stripping tower oil inlet (71), the top end of the stripping tower (7) is provided with a stripping tower heat conduction port (72), and the lower part of the stripping tower (7) is provided with a stripping tower oil outlet (73);
the side wall of the drying tower (9) is provided with a drying tower oil inlet (92), the top end of the drying tower (9) is provided with a drying tower heat conduction port (91), and the lower end of the drying tower (9) is provided with a drying tower oil outlet (93);
the condenser comprises a first condenser (51), a second condenser (52) and a third condenser (53), a first oil outlet (11) is connected with a middle oil inlet (210), a first solvent outlet (12), a flash evaporation solvent outlet (233) and a second solvent outlet (42) are respectively connected with the first condenser (51) and the second condenser (52), a drying tower heat conduction port (91), a stripping tower heat conduction port (72) and the third condenser (53) are connected to a heat conduction port (213), a middle solvent outlet (212) is connected with the third condenser (53), a middle pump (24) is connected with a heat exchanger (3), the heat exchanger (3) is connected with a second oil inlet (41), a second oil outlet (43) is connected with a stripping tower oil inlet (71) through a stripping tower oil pump (6), and an oil outlet (73) is connected with a drying tower oil inlet (92) through a second oil pump (8), an oil outlet (93) of the drying tower is connected with a tail end pump.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022623418.1U CN213823507U (en) | 2020-11-13 | 2020-11-13 | Evaporating device and miscella evaporating device in middle of miscella |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022623418.1U CN213823507U (en) | 2020-11-13 | 2020-11-13 | Evaporating device and miscella evaporating device in middle of miscella |
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| CN213823507U true CN213823507U (en) | 2021-07-30 |
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| CN202022623418.1U Active CN213823507U (en) | 2020-11-13 | 2020-11-13 | Evaporating device and miscella evaporating device in middle of miscella |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
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