CN114470841A - Heat energy recovery equipment for pre-dipping workshop section - Google Patents
Heat energy recovery equipment for pre-dipping workshop section Download PDFInfo
- Publication number
- CN114470841A CN114470841A CN202210255803.6A CN202210255803A CN114470841A CN 114470841 A CN114470841 A CN 114470841A CN 202210255803 A CN202210255803 A CN 202210255803A CN 114470841 A CN114470841 A CN 114470841A
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- China
- Prior art keywords
- evaporator
- heat exchanger
- stripping tower
- outlet
- energy recovery
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- 238000011084 recovery Methods 0.000 title claims abstract description 15
- 238000007598 dipping method Methods 0.000 title claims description 3
- 239000003921 oil Substances 0.000 claims abstract description 24
- 239000010779 crude oil Substances 0.000 claims abstract description 17
- 238000002791 soaking Methods 0.000 claims abstract description 10
- 241000237983 Trochidae Species 0.000 claims abstract description 3
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000008157 edible vegetable oil Substances 0.000 abstract description 2
- 239000002904 solvent Substances 0.000 description 9
- 239000000126 substance Substances 0.000 description 4
- 235000019764 Soybean Meal Nutrition 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 238000003915 air pollution Methods 0.000 description 3
- 238000002386 leaching Methods 0.000 description 3
- 235000012054 meals Nutrition 0.000 description 3
- 239000004455 soybean meal Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
Images
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
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
-
- 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
- B01D3/38—Steam distillation
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/12—Refining fats or fatty oils by distillation
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/12—Refining fats or fatty oils by distillation
- C11B3/14—Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Microbiology (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to edible oil production equipment, in particular to heat energy recovery equipment for a pre-soaking section. The heat energy recovery equipment for the pre-soaking section comprises a first evaporator, a second evaporator, a desolventizer-toaster, a stripping tower and a heat exchanger; the top of the desolventizer-toaster is connected with the top shell pass of the first evaporator; the top of the stripping tower is connected with a second evaporator, and the bottom of the stripping tower is connected with a crude oil cooler; and a top steam outlet of the stripping tower or a top steam outlet of the second evaporator is connected with a shell side inlet of the newly-added heat exchanger, a tube side inlet of the heat exchanger is connected with an oil outlet of the first evaporator, and a tube side outlet of the heat exchanger is connected with a tube side inlet of the second evaporator. According to the invention, the mixed oil which is pre-input into the second evaporator is preheated by adopting the top steam of the second evaporator or the stripping tower, and the preheated mixed oil directly enters the second evaporator, so that the consumption of the steam in the second evaporator is reduced, and the secondary utilization of heat energy is realized.
Description
Technical Field
The invention relates to edible oil production equipment, in particular to heat energy recovery equipment for a pre-soaking section.
Background
The solvent residue of the soybean meal is an important index of solvent consumption and soybean meal amount of an oil extraction plant, the desolventizing effect of wet meal directly influences the solvent consumption and the solvent residue of finished soybean meal, and when the residual dissolution exceeds the standard, the solvent consumption is increased, the feeding value is reduced, and even the death of animals can be caused.
The wet meal generated in the oil leaching workshop has about 25-35% of solvent residues, and the solvent generally exists in the forms of mechanical combination, chemical combination and physical-chemical combination, wherein the solvent amount combined in the chemical and physical-chemical modes is small and is difficult to remove, and the key point of wet meal desolventization is. Although the performance of the existing desolventizer-toaster is gradually improved, the existing domestic advanced desolventizer-toaster generally modifies a DT desolventizer-toaster or a DTDC desolventizer-toaster, mainly researches the height of a desolventizer-toaster section, the steam state and the exhaust mode, and is still deficient in the aspects of how to effectively reduce the heat source consumption and the power consumption in the desolventizing process, and the utilization of the heat energy generated in the desolventizing step.
The heat energy recovery of the leaching workshop is a process for recovering the heat energy of the leaching workshop, main matched equipment comprises a desolventizer-toaster, a pump, a valve and the like, and steam evaporated and absorbed in the existing desolventizer-toaster, an evaporator and a stripping tower is often discharged into the atmosphere to pollute the atmosphere; or the steam is directly input into the condenser for cooling, thereby not only increasing the load of the condenser but also wasting heat energy, and not achieving the effects of saving energy and steam.
Disclosure of Invention
In view of the above problems, an object of the present invention is to provide a heat energy recovery apparatus for a pre-soaking section, wherein a part of the mixed oil pre-fed into a second evaporator is preheated by using the steam at the top of the second evaporator or a stripping tower, and on one hand, the mixed oil directly enters the second evaporator after being preheated, so that the consumption of the steam in the second evaporator is reduced, and the production cost is saved; and on the other hand, the top steam of the second evaporator or the stripping tower is secondarily utilized, so that the air pollution is reduced. In addition, the direct input of the overhead vapor of the second evaporator or stripper into the condenser is also avoided, which aggravates the work load of the condenser.
The technical purpose of the invention is realized by the following technical scheme, and the heat energy recovery equipment for the pre-soaking section comprises:
an evaporation device comprising a first evaporator and a second evaporator;
the top of the desolventizer-toaster is connected with the top shell pass of the first evaporator;
the top of the stripping tower is connected with the second evaporator, and the bottom of the stripping tower is connected with a crude oil cooler;
the steam-assisted stripping tower comprises a heat exchanger, wherein a top steam outlet of the stripping tower or a top steam outlet of the second evaporator is connected with a shell side inlet of the heat exchanger, a tube side inlet of the heat exchanger is connected with an oil outlet of the first evaporator, and a tube side outlet of the heat exchanger is connected with the second evaporator.
In one embodiment, a condenser is connected to the shell side outlet of the heat exchanger, and the top steam outlet of the first evaporator is connected with the condenser.
In one embodiment, when the top vapor outlet of the stripping column is connected to the shell-side inlet of the heat exchanger, the top vapor outlet of the second evaporator is connected to the condenser; and when the top steam outlet of the second evaporator is connected with the shell side inlet of the heat exchanger, the top steam outlet of the stripping tower is connected with the condenser.
In one embodiment, the heat exchanger is a tube-plate heat exchanger, the tube-side medium of the heat exchanger is mixed oil, and the shell-side medium of the heat exchanger is the overhead steam of the second evaporator or the stripping column.
In one embodiment, one end of the crude oil cooler is connected with a crude oil tank.
The invention has the advantages that:
(1) according to the invention, the top steam of the second evaporator or the stripping tower is adopted to preheat part of the mixed oil which is pre-input into the second evaporator, and the preheated mixed oil is directly input into the second evaporator, so that the consumption of the steam in the second evaporator is reduced, and the production cost is saved; in addition, the secondary utilization of the steam at the top of the second evaporator or stripping tower is realized.
(2) In the invention, the top steam generated by the second evaporator or the stripping tower is directly input into the heat exchanger for heat exchange, so that the temperature is reduced after heat exchange, and the workload of a subsequent condenser is reduced; in addition, the condenser is adopted to condense the steam, so that air pollution is reduced.
(3) The heat energy recovery equipment for the pre-soaking section provided by the invention is 100m2The heat exchanger is taken as an example, the steam saving amount can reach about 500kg/h, and the steam is saved by about 12 tons per day.
Drawings
FIG. 1 is a schematic structural view of example 1 of the present invention;
fig. 2 is a schematic structural diagram of embodiment 2 of the present invention.
In the figure, 1, a desolventizer-toaster; 2. a stripping column; 3. a first evaporator; 4. a second evaporator; 5. a heat exchanger; 6. a crude oil cooler; 7. a crude oil tank; 8. a condenser.
Detailed Description
Example 1
As shown in figure 1, the heat energy recovery equipment for the pre-soaking section comprises an evaporation device, a desolventizer-toaster 1, a stripping tower 2 and a crude oil cooler 6. The evaporation device comprises a first evaporator 3 and a second evaporator 4, the top of the desolventizer-toaster 1 is connected with the shell side at the top of the first evaporator 3 through a pipeline, the tube side of the second evaporator 4 is connected with the top of the stripping tower 2 through a pipeline, and the bottom of the stripping tower 2 is connected with the crude oil cooler 6 through a pipeline. The top steam outlet of the stripping tower 2 is connected with the shell side inlet of the heat exchanger 5 through a pipeline, the tube side inlet of the heat exchanger 5 is connected with the oil outlet of the first evaporator 3 through a pipeline, and the tube side outlet of the heat exchanger 5 is connected with the tube side inlet of the second evaporator 4 through a pipeline.
Further, a shell side outlet of the heat exchanger 5 is connected with an inlet of the condenser 8 through a pipeline, a top steam outlet of the first evaporator 3 is connected with an inlet of the condenser 8 through a pipeline, and a top steam outlet of the second evaporator 4 is connected with an inlet of the condenser 8.
Further, the heat exchanger 5 is a tube-plate heat exchanger, the tube-side medium of the heat exchanger 5 is mixed oil, and the shell-side medium of the heat exchanger 5 is top steam of the stripping tower 2.
Further, a crude oil tank 7 is connected to the end of the crude oil cooler 6 remote from the stripping tower 2.
Example 2
This example differs from example 1 in that: the top steam outlet of the second evaporator 4 is connected with the shell side inlet of the heat exchanger 5 through a pipeline, and the top steam outlet of the stripping tower 2 is connected with the inlet of the condenser 8.
The working principle of the invention is as follows: the mixed oil is input into the tube side of the first evaporator 3 through the bottom of the first evaporator 3, the desolventizer-toaster 1 is connected with the shell side of the first evaporator 3, the shell side of the first evaporator 3 adopts the top steam, the direct steam, the cooking pot and the like of the desolventizer-toaster 1 as heating heat sources, and in the first evaporator 3, the top steam of the desolventizer-toaster 1 heats the mixed oil to change the liquid solvent in the mixed oil into gas to be primarily separated from the first evaporator 3. And then the mixed oil in the first evaporator 3 is input into a heat exchanger 5 under the action of a pump, the steam at the top of the second evaporator 4 or the stripping tower 2 enters the heat exchanger 5 to preheat the mixed oil, and the preheated mixed oil directly enters the tube pass of the second evaporator 4 through a tube pass outlet of the heat exchanger 5 to be heated under the action of the pump. The top steam in the heat exchanger 5 enters the condenser 8 through the shell side outlet of the heat exchanger 5 for condensation. Indirect steam is adopted as a heating heat source in the shell pass of the second evaporator 4, the mixed oil concentrated by the second evaporator 4 is input into the stripping tower 2 under the action of a pump, the mixed oil and the direct steam sprayed from the bottom of the stripping tower 2 are subjected to countercurrent stripping, crude oil extracted from the bottom of the stripping tower 2 is obtained, and the crude oil extracted is condensed by the crude oil cooler 6 and then enters the crude oil tank 7 for storage, and the subsequent refining is waited. On one hand, the invention preheats part of the mixed oil which is pre-input into the second evaporator 4 by adopting the steam at the top of the second evaporator 4 or the stripping tower 2, thereby reducing the consumption of the steam in the second evaporator 4 and saving the production cost; on the other hand, the top steam in the second evaporator 4 or the stripping tower 2 is secondarily utilized, so that the air pollution is reduced; in addition, the overhead steam temperature of the second evaporator 4 or the stripping column 2 can be reduced, and the work load of the subsequent condenser 8 can be reduced.
It will be apparent to those skilled in the art that various other changes and modifications may be made in the above-described embodiments and concepts and all such changes and modifications are intended to be within the scope of the appended claims.
Claims (5)
1. A heat energy recovery device for a pre-soaking section is characterized by comprising:
an evaporation device comprising a first evaporator (3) and a second evaporator (4);
the top of the desolventizer-toaster (1) is connected with the top shell pass of the first evaporator (3);
the top of the stripping tower (2) is connected with the second evaporator (4), and the bottom of the stripping tower (2) is connected with a crude oil cooler (6);
the steam-water separator comprises a heat exchanger (5), wherein a top steam outlet of the stripping tower (2) or a top steam outlet of the second evaporator (4) is connected with a shell side inlet of the heat exchanger (5), a tube side inlet of the heat exchanger (5) is connected with an oil outlet of the first evaporator (3), and a tube side outlet of the heat exchanger (5) is connected with the second evaporator (4).
2. The heat energy recovery equipment for the pre-soaking section according to the claim 1, characterized in that a condenser (8) is connected to the shell side outlet of the heat exchanger (5), and the top steam outlet of the first evaporator (3) is connected with the condenser (8).
3. The pre-dip section heat energy recovery plant according to claim 1, characterized in that the top steam outlet of the second evaporator (4) is connected with the condenser (8) when the top steam outlet of the stripping tower (2) is connected with the shell side inlet of the heat exchanger (5); when the top steam outlet of the second evaporator (4) is connected with the shell side inlet of the heat exchanger (5), the top steam outlet of the stripping tower (2) is connected with the condenser (8).
4. The heat energy recovery equipment for the pre-dipping workshop section according to claim 1, wherein the heat exchanger (5) is a tube-plate heat exchanger, the tube-side medium of the heat exchanger (5) is mixed oil, and the shell-side medium of the heat exchanger (5) is the overhead steam of the second evaporator (4) or the stripping tower (2).
5. The heat energy recovery equipment for the pre-soaking sections according to the claim 1, characterized in that one end of the crude oil cooler (6) is connected with a crude oil tank (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210255803.6A CN114470841A (en) | 2022-03-15 | 2022-03-15 | Heat energy recovery equipment for pre-dipping workshop section |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210255803.6A CN114470841A (en) | 2022-03-15 | 2022-03-15 | Heat energy recovery equipment for pre-dipping workshop section |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN114470841A true CN114470841A (en) | 2022-05-13 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210255803.6A Pending CN114470841A (en) | 2022-03-15 | 2022-03-15 | Heat energy recovery equipment for pre-dipping workshop section |
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| Country | Link |
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| CN (1) | CN114470841A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204745703U (en) * | 2015-05-21 | 2015-11-11 | 迈安德集团有限公司 | Mix liquid vaporization system |
| CN213823507U (en) * | 2020-11-13 | 2021-07-30 | 九三粮油工业集团有限公司 | Evaporating device and miscella evaporating device in middle of miscella |
| CN214088436U (en) * | 2020-11-30 | 2021-08-31 | 迈安德集团有限公司 | Mixed oil evaporation desolventizing system |
| CN214260711U (en) * | 2020-11-13 | 2021-09-24 | 九三粮油工业集团有限公司 | Negative pressure evaporation system for secondary steam utilization of stripping tower |
-
2022
- 2022-03-15 CN CN202210255803.6A patent/CN114470841A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN204745703U (en) * | 2015-05-21 | 2015-11-11 | 迈安德集团有限公司 | Mix liquid vaporization system |
| CN213823507U (en) * | 2020-11-13 | 2021-07-30 | 九三粮油工业集团有限公司 | Evaporating device and miscella evaporating device in middle of miscella |
| CN214260711U (en) * | 2020-11-13 | 2021-09-24 | 九三粮油工业集团有限公司 | Negative pressure evaporation system for secondary steam utilization of stripping tower |
| CN214088436U (en) * | 2020-11-30 | 2021-08-31 | 迈安德集团有限公司 | Mixed oil evaporation desolventizing system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
| CN115253348B (en) * | 2022-07-11 | 2023-10-20 | 山东凯斯达机械制造有限公司 | Evaporation device and technology for mixed oil of leaching system |
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Application publication date: 20220513 |