CN212270053U - Grease hydrolysis device - Google Patents
Grease hydrolysis device Download PDFInfo
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- CN212270053U CN212270053U CN202020207599.7U CN202020207599U CN212270053U CN 212270053 U CN212270053 U CN 212270053U CN 202020207599 U CN202020207599 U CN 202020207599U CN 212270053 U CN212270053 U CN 212270053U
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Abstract
The utility model provides a grease hydrolysis unit belongs to fatty acid production technical field, include: the heat exchange tower is used for heat exchange of the raw material and the hydrolysate and separation of the hydrolysate; the hydrolysis reaction tower is used for reacting raw materials, is communicated with the heat exchange tower and is used for the reaction of the raw materials in the hydrolysis reaction tower, and the hydrolysis products are subjected to heat exchange and separation in the heat exchange tower; and the heating furnace is communicated between the heat exchange tower and the hydrolysis reaction tower so as to enable the raw materials entering the hydrolysis reaction tower to be in a gas phase. The utility model discloses can realize the low pressure continuous hydrolysis of grease, reduce equipment cost, and improve the safety in production condition.
Description
Technical Field
The utility model belongs to the technical field of fatty acid production, concretely relates to grease hydrolysis unit.
Background
The traditional methods for hydrolyzing the grease comprise an acidification method, a medium-high pressure hydrolysis method and the like. The acidification method has the advantages of large wastewater treatment load, high pollution discharge and treatment strength and low hydrolysis rate. Although the medium-high pressure hydrolysis method has high hydrolysis rate, high-temperature and high-pressure steam needs to be supplied externally to meet the temperature and pressure required by the hydrolysis process, and the reason why the medium-high pressure hydrolysis method cannot be popularized widely is the huge investment and the overhigh operation cost formed by a high-pressure system of a production device.
SUMMERY OF THE UTILITY MODEL
Based on the above background problem, the utility model aims at providing a grease hydrolysis unit can realize the low pressure of grease and hydrolysise in succession, has reduced equipment cost, and has improved the safety in production condition.
In order to achieve the above object, the embodiment of the present invention provides a technical solution:
a fat hydrolysis device comprising: the heat exchange tower is used for heat exchange of the raw material and the hydrolysate and separation of the hydrolysate; the hydrolysis reaction tower is used for reacting raw materials, is communicated with the heat exchange tower and is used for the reaction of the raw materials in the hydrolysis reaction tower, and the hydrolysis products are subjected to heat exchange and separation in the heat exchange tower; and the heating furnace is communicated between the heat exchange tower and the hydrolysis reaction tower so as to enable the raw materials entering the hydrolysis reaction tower to be in a gas phase.
The top end of the heat exchange tower is communicated with the heating furnace so that the raw materials after heat exchange enter the heating furnace to be heated into a gas phase, and the heating furnace is communicated with the top end of the hydrolysis reaction tower so that the gas phase raw materials enter the hydrolysis reaction tower.
In one embodiment, a heat exchanger and a separator which are communicated are arranged in the heat exchange tower, the heat exchanger is arranged above the separator, and the bottom of the heat exchanger is communicated with a first raw material inlet so as to supply grease to enter for heat exchange.
Wherein the temperature in the heat exchanger is 40-380 ℃, and the temperature of the heating furnace is 300-380 ℃.
The top of the separator is communicated with a gas product outlet, the bottom of the separator is communicated with a liquid product outlet, and the bottom end of the separator is also communicated with a slag discharge port.
In one embodiment, a cooler is arranged between the heat exchanger and the separator, and the temperature in the cooler is 40-60 ℃.
Preferably, the heat exchange column has a diameter of 0.6 to 1.2m and a height of 8 to 18 m.
In one embodiment, a hydrolyzer and an evaporator are arranged in the hydrolysis reaction tower, the hydrolyzer is arranged above the evaporator, and the bottom of the hydrolyzer is communicated with a second raw material inlet for water to enter and be vaporized by the evaporator.
Wherein the pressure in the hydrolyzer is 0.06-0.08MPa, and the temperature is 330-380 ℃; the pressure in the evaporator is 0.06-0.08MPa, and the temperature is 330-380 ℃.
Preferably, the hydrolysis reaction tower has a diameter of 0.8 to 3m and a height of 8 to 18 m.
Compared with the prior art, the embodiment of the utility model provides a have following effect at least:
1. the utility model discloses a pressure that the device of hydrolysising can control whole hydrolysis process is between 0.06-0.08MPa, is far less than traditional medium and high pressure hydrolysis method's pressure 5.5MPa, and the temperature of whole hydrolysis process is at 30-380 ℃, belongs to middle and low temperature operating condition, and whole hydrolysis process is continuous steady, safe and reliable.
2. The utility model discloses remove high pressure boiler heat supply mode, the hydrolysis reaction heat is supplied with by hydrolysate waste heat recovery and heating furnace, has got rid of high pressure boiler and high pressure reactor, has reduced equipment cost, has improved the safety in production condition.
3. The utility model discloses a hydrolysis unit can integrate, the modularization, is convenient for realize standardization, normalization to be favorable to promoting.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly described below.
FIG. 1 is a schematic structural diagram of a device for hydrolyzing oil in example 1 of the present invention;
FIG. 2 is a schematic structural diagram of a device for hydrolyzing oil in example 2 of the present invention;
fig. 3 is a schematic structural diagram of a device for hydrolyzing oil in embodiment 3 of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "top", "bottom", "left", "right", "vertical", "horizontal", "inner", "outer", "front", "rear", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings of the specification, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. In the description of the present invention, it should be noted that the terms "first", "second" and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Example 1
A grease hydrolyzing device, as shown in FIG. 1, comprises: the hydrolysis reaction device comprises a heat exchange tower 1, a hydrolysis reaction tower 2 and a heating furnace 3, wherein the heating furnace 3 is communicated between the heat exchange tower 1 and the hydrolysis reaction tower 2, on one hand, raw materials conveyed from the heat exchange tower 1 are in a gas phase and enter the hydrolysis reaction tower 2 for hydrolysis, on the other hand, hydrolysis products generated by reaction enter the heat exchange tower 1 for heat exchange, and therefore two paths of conveying pipelines are arranged between the heat exchange tower 1 and the hydrolysis reaction tower 2.
Specifically, a first raw material inlet 101 and a raw material outlet 102 are formed in the side wall of the heat exchange tower 1, the first raw material inlet 101 is arranged below the raw material outlet 102, raw materials such as grease and catalyst enter the heat exchange tower 1 from the first raw material inlet 101 through a raw material pump (not shown in the figure) for heat exchange, the temperature of the raw material inlet is 40-50 ℃, and the temperature of the raw material is increased to 120-180 ℃ after heat exchange in the heat exchange tower 1. The top end of the heat exchange tower 1 is communicated with the heating furnace 3 so that the raw materials after heat exchange enter the heating furnace 3 to be heated into gas phase, and the heating furnace 3 is communicated with the top end of the hydrolysis reaction tower 2 so that the gas phase raw materials enter the hydrolysis reaction tower 2.
The gas phase raw material entering the hydrolysis reaction tower 2 contacts and reacts with the water vapor in the hydrolysis reaction tower 2 to obtain a hydrolysis product, the gas phase in the obtained hydrolysis product enters the heat exchange tower 1 from the hydrolysis reaction tower 2 for heat exchange, the initial temperature is 330-380 ℃, and the temperature is reduced to 160-280 ℃ after the heat exchange in the heat exchange tower 1. The power for conveying the hydrolysis product comes from pressure difference, the pressure in the hydrolysis reaction tower 2 is 0.06-0.08MPa, and the pressure in the heat exchange tower 1 is 0.015-0.03MPa, so that the gas phase of the hydrolysis product enters the heat exchange tower 1 along the conveying pipeline for heat exchange under the action of the pressure difference, and the hydrolysis reaction is continuous, so that the hydrolysis product entering the heat exchange tower 1 exchanges heat with the subsequently entering raw material, and the cooling is realized.
In this embodiment, as shown in fig. 1, a first manhole 201 is opened at the top end of the hydrolysis reaction tower 2, a second manhole 202 is opened at the upper portion, a third manhole 203 is opened at the bottom, a first liquid meter port 204 is opened at the bottom of the hydrolysis reaction tower 2, and a second liquid meter port 103 is also opened at the bottom of the heat exchange tower 1.
The utility model discloses a carry out hydrolysis reaction again after vaporizing raw materials to with pressure control within 0.08MPa, be less than well high pressure hydrolysis's operating pressure far away, not only can reduce equipment cost and drop into, can guarantee production safe and reliable moreover.
Example 2
This embodiment provides a grease hydrolysis device, as shown in fig. 2, including: the hydrolysis reaction device comprises a heat exchange tower, a hydrolysis reaction tower and a heating furnace 1, wherein the top end of the heat exchange tower is communicated with the heating furnace 1, the heating furnace 1 is communicated with the top end of the hydrolysis reaction tower, namely the heating furnace 1 is communicated between the heat exchange tower and the hydrolysis reaction tower, on one hand, raw materials conveyed from the heat exchange tower are in a gas phase and enter the hydrolysis reaction tower for hydrolysis, on the other hand, hydrolysis products generated by reaction enter the heat exchange tower for hydrolysis, and therefore two paths of conveying pipelines are arranged between the heat exchange tower and the hydrolysis reaction tower.
Specifically, a heat exchanger 2 and a separator 3 which are communicated are arranged in the heat exchange tower, the heat exchanger 2 is arranged above the separator 3, the bottom of the heat exchanger 2 is communicated with a first raw material inlet 201, the top of the heat exchanger 2 is communicated with a raw material outlet 202, raw materials such as grease and partial catalyst enter the heat exchanger 2 from the first raw material inlet 201 through a raw material pump for heat exchange, specifically, the raw materials exchange heat with a hydrolysate which is described later, the temperature of the raw material inlet is 40-50 ℃, and the temperature of the raw materials is increased to 120-plus-180 ℃ after heat exchange through the heat exchanger 2. The heat exchanger 2 is a shell and tube heat exchanger in this embodiment, but is not limited thereto.
The raw material after heat exchange by the heat exchanger 2 enters the heating furnace 1 to be heated into a gas phase, the temperature in the heating furnace 1 is 300-380 ℃, and the gas phase raw material is continuously conveyed into the hydrolysis reaction tower.
In this embodiment, a hydrolyzer 4 and an evaporator 5 are arranged in the hydrolysis reaction tower, the hydrolyzer 4 is arranged above the evaporator 5, the bottom of the hydrolyzer 4 is communicated with a second raw material inlet 401 for water and part of the catalyst to enter and vaporize through the evaporator 5, and the vaporized raw materials such as water contact with the gas-phase raw materials to perform hydrolysis reaction to generate hydrolysis products.
Specifically, three second raw material inlets 401 are provided, and the three second raw material inlets 401 are distributed up and down; the pressure in the hydrolyzer 4 is 0.06-0.08MPa, the temperature is 330-380 ℃, the pressure in the evaporator 5 is 0.06-0.08MPa, and the temperature is 330-380 ℃. Namely, the utility model discloses within the pressure 0.08MPa that can control the hydrolysis reaction, be far less than the operating pressure of medium-high pressure hydrolysis method, not only can reduce equipment cost and drop into, can guarantee production safe and reliable moreover.
Because the pressure of the hydrolyzer 4 is higher than that of the heat exchanger 2, the gas phase in the hydrolysate returns to the heat exchanger 2 from the hydrolyzer 4 to exchange heat with the newly conveyed raw material for cooling under the driving of pressure difference, the initial temperature of the gas phase of the hydrolysate is 330-380 ℃, the temperature is reduced to 160-280 ℃ after heat exchange by the heat exchanger 2, and the cooled hydrolysate enters the separator 3 for separation.
In this embodiment, the top of the separator 3 is communicated with a gas product outlet 301, the bottom of the separator 3 is communicated with a liquid product outlet 302, and the bottom of the separator 3 is further communicated with a slag discharge port 303. The separated fuel gas is discharged from the gaseous product outlet 301 and the mixed fatty acid is discharged from the liquid product outlet 302. Specifically, the operating pressure of the separator 3 was 0.015MPa, and the temperature was 60 ℃.
The pressure of the whole hydrolysis process of the embodiment is between 0.03 and 0.08MPa, which is far lower than the pressure of the traditional medium-high pressure hydrolysis method by 5.5MPa, the temperature of the whole hydrolysis process is between 30 and 380 ℃, the method belongs to the medium-low temperature operation condition, and the whole process is continuous, stable, safe and reliable.
In the embodiment, the diameter of the heat exchange tower is 0.6-1.2m, the height is 8-18m, the diameter of the hydrolysis reaction tower is 0.8-3m, and the height is 8-18m, and specific size parameters can be adjusted according to the use condition.
Example 3
It should be noted that, in the utility model, heat exchanger, separator, hydrolyzer, evaporator, cooler, heating furnace etc. be current product, its concrete structure this embodiment will not be repeated again.
In addition, the utility model discloses not only can be used for the hydrolysis of grease, can also be used for the processing and treatment of saponin.
It should be noted that, for those skilled in the art, without departing from the inventive concept, several variations and modifications can be made, which are within the scope of the present invention.
Claims (10)
1. A grease hydrolyzing device, comprising:
the heat exchange tower is used for heat exchange of the raw material and the hydrolysate and separation of the hydrolysate;
the hydrolysis reaction tower is used for reacting raw materials, is communicated with the heat exchange tower and is used for the reaction of the raw materials in the hydrolysis reaction tower, and the hydrolysis products are subjected to heat exchange and separation in the heat exchange tower;
and the heating furnace is communicated between the heat exchange tower and the hydrolysis reaction tower so as to enable the raw materials entering the hydrolysis reaction tower to be in a gas phase.
2. The grease hydrolyzing device according to claim 1, wherein the top end of the heat exchange tower is communicated with a heating furnace so that the heat-exchanged raw materials enter the heating furnace to be heated into a gas phase, and the heating furnace is communicated with the top end of the hydrolysis reaction tower so that the gas-phase raw materials enter the hydrolysis reaction tower.
3. The grease hydrolysis device according to claim 2, wherein a heat exchanger and a separator which are communicated with each other are arranged in the heat exchange tower, the heat exchanger is arranged above the separator, and a first raw material inlet is communicated with the bottom of the heat exchanger to allow grease to enter for heat exchange.
4. The grease hydrolyzing device according to claim 3, wherein the temperature in the heat exchanger is 40-380 ℃, and the temperature in the heating furnace is 300-380 ℃.
5. The grease hydrolyzing device according to claim 3, wherein the top of the separator is communicated with a gas product outlet, the bottom of the separator is communicated with a liquid product outlet, and the bottom end of the separator is also communicated with a slag discharge port.
6. The grease hydrolyzing device according to claim 3, wherein a cooler is further provided between the heat exchanger and the separator, and the temperature in the cooler is 40-60 ℃.
7. The fat hydrolysis apparatus as set forth in claim 1, wherein the heat exchange tower has a diameter of 0.6 to 1.2m and a height of 8 to 18 m.
8. The grease hydrolyzing device according to claim 2, wherein a hydrolyzer and an evaporator are arranged in the hydrolysis reaction tower, the hydrolyzer is arranged above the evaporator, and the bottom of the hydrolyzer is communicated with a second raw material inlet for water to enter and be vaporized by the evaporator.
9. The grease hydrolyzing device as claimed in claim 8, wherein the pressure in the hydrolyzer is 0.06-0.08MPa, and the temperature is 330-380 ℃; the pressure in the evaporator is 0.06-0.08MPa, and the temperature is 330-380 ℃.
10. The grease hydrolyzing device according to claim 1, wherein the hydrolysis reaction tower has a diameter of 0.8 to 3m and a height of 8 to 18 m.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020207599.7U CN212270053U (en) | 2020-02-25 | 2020-02-25 | Grease hydrolysis device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020207599.7U CN212270053U (en) | 2020-02-25 | 2020-02-25 | Grease hydrolysis device |
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| CN212270053U true CN212270053U (en) | 2021-01-01 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111171963A (en) * | 2020-02-25 | 2020-05-19 | 珠海天汇能源科技有限公司 | Grease hydrolysis device and grease hydrolysis method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111171963A (en) * | 2020-02-25 | 2020-05-19 | 珠海天汇能源科技有限公司 | Grease hydrolysis device and grease hydrolysis method |
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