CN212174844U - Furfural refining device supporting wide solvent-oil ratio operation conditions - Google Patents
Furfural refining device supporting wide solvent-oil ratio operation conditions Download PDFInfo
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- CN212174844U CN212174844U CN202020607826.5U CN202020607826U CN212174844U CN 212174844 U CN212174844 U CN 212174844U CN 202020607826 U CN202020607826 U CN 202020607826U CN 212174844 U CN212174844 U CN 212174844U
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Abstract
The utility model relates to a furfural refining device supporting wide solvent-oil ratio operating conditions, which comprises a degassing tower, an extraction tower, an evaporation tower, a waste liquid flash stripping tower, a drying tower and a waste liquid furnace; the evaporation tower is internally divided into a first-effect unit, a third-effect unit and a second-effect unit from top to bottom; the bottom outlet of the degassing tower is connected with an extraction tower, and the bottom outlet of the extraction tower is connected with a first-effect unit of an evaporation tower; the top outlet of the first-effect unit of the evaporation tower is connected with the drying tower, the bottom outlet of the first-effect unit of the evaporation tower is connected with the second-effect unit of the evaporation tower, the bottom outlet of the second-effect unit of the evaporation tower is connected with the waste liquid furnace, the waste liquid furnace is connected with the third-effect unit of the evaporation tower, and the bottom outlet of the third-effect unit of the evaporation tower is connected with the waste liquid flash evaporation stripping tower; the top outlet of the waste liquid flash evaporation stripping tower is connected with the drying tower; and the outlet at the bottom of the drying tower is connected with an eighth delivery pump, and the eighth delivery pump is respectively connected with the first-effect unit and the second-effect unit of the extraction tower and the evaporator through three pipelines.
Description
Technical Field
The utility model relates to a petrochemical apparatus, especially relate to a support wide agent oil ratio operating condition's furfural refining plant.
Background
The furfural refining device is one of key devices for producing products such as rubber plasticizer, transformer oil and the like, the device utilizes a furfural solvent with strong selectivity and weak dissolving capacity to have different solubilities on different hydrocarbons in petroleum atmospheric and vacuum distillate oil, aromatic hydrocarbons with multiple rings and short side chains and naphthenic hydrocarbons, colloid, sulfur and nitrogen compounds (all non-ideal components) have large solubilities in furfural, and hydrocarbons with fewer rings and long side chains (ideal components needing to be enriched) have small solubilities in furfural. According to the difference of the boiling points of furfural and oil products containing non-ideal components, the furfural and extract oil are separated by heating-evaporation.
Different products can be obtained according to different raw materials and operation conditions: hydrogenated three-line distillate oil is used as a raw material, the solvent-oil ratio is 0.5-1.2, and a furfural refining device can be used for producing the rubber plasticizer; the hydrogenation normal second-line distillate oil is used as a raw material, the solvent-oil ratio is 2.0-3.0, and a furfural refining device can be used for obtaining the transformer oil base oil.
If the alternative production of the two products by using one set of furfural refining device can be realized, the use efficiency of the device can be improved, the production cost can be reduced, and the economic benefit can be greatly improved. However, because the difference between the solvent-oil ratios required for producing different products is large, and the design values of the solvent-oil ratios of the furfural refining device are fixed values, the alternative production of different products by using one set of device has great technical difficulty: when the solvent-oil ratio is smaller than a design value, the quantity of the produced extract is small, the production safety is affected by the temperature runaway phenomenon after the small quantity of extract enters the heating furnace, and the furfural obtained by separation is small and is easy to cause coking to block a pipeline; in addition, during production, heat in the furfural needs to be recovered and transferred to the raw material through a heat exchanger, and the small amount of furfural is not enough to raise the temperature of the raw material to the ideal temperature, so that the heat balance is broken; finally, when the amount of the extract is small, the liquid level of the evaporation tower is low, the normal operation of a pump is influenced, and the stability of the whole solvent recovery system is influenced.
Under the prior art condition, in order to produce products with different dosages and oil ratios, a plurality of sets of furfural refining devices need to be repeatedly built, and resource waste is caused.
Disclosure of Invention
To the problem, the utility model aims at providing a support wide agent oil ratio operating condition's furfural refining plant, the device can produce different agent oil ratio products in turn, improves device availability factor, and reduction in production cost improves economic benefits by a wide margin.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a furfural refining device supporting wide solvent-oil ratio operating conditions comprises a degassing tower, an extraction tower, an evaporation tower, a waste liquid flash evaporation stripping tower, a drying tower and a waste liquid furnace; the evaporation tower is internally divided into a first-effect unit, a third-effect unit and a second-effect unit from top to bottom;
the bottom outlet of the degassing tower is connected with the extraction tower through a first pipeline, and the top outlet of the degassing tower discharges aldehyde-water mixed gas; the bottom outlet of the extraction tower is connected with the primary effect unit of the evaporation tower through a second pipeline, and the top outlet of the extraction tower discharges refined oil; the top outlet of the first-effect unit of the evaporation tower is connected with the drying tower through a third pipeline, the bottom outlet of the first-effect unit of the evaporation tower is connected with the second-effect unit of the evaporation tower through a fourth pipeline, the bottom outlet of the second-effect unit of the evaporation tower is connected with a waste liquid furnace through a fifth pipeline, the waste liquid furnace is connected with the third-effect unit of the evaporation tower through a sixth pipeline, and the bottom outlet of the third-effect unit of the evaporation tower is connected with the waste liquid flash evaporation stripping tower through a seventh pipeline; the top outlet of the waste liquid flash stripping tower is connected with the drying tower through an eighth pipeline, and the bottom outlet of the waste liquid flash stripping tower discharges extract oil; and an outlet at the top of the drying tower discharges aldehyde-water mixed gas, an outlet at the bottom of the drying tower is connected with an eighth delivery pump, and the eighth delivery pump is respectively connected with the extraction tower, the primary effect unit and the secondary effect unit of the evaporator through three pipelines.
Preferably, a seventh valve is provided on a line between the eighth transfer pump and the extraction column; a second remote control valve and a second flow meter are arranged on a pipeline between the eighth delivery pump and the primary effect unit of the evaporator; a first remote control valve and a first flow meter are provided on a line between the eighth transfer pump and the secondary effect unit of the evaporator.
Preferably, the degassing tower is connected with a raw material conveying pipeline, and a first conveying pump and a first valve are arranged on the raw material conveying pipeline; a second valve and a second delivery pump are arranged on the first pipeline; a third valve and a first heat exchanger are arranged on the second pipeline; a ninth delivery pump, a second heat exchanger and an eighth valve are arranged on the fourth pipeline; a fourth valve and a fourth delivery pump are arranged on the fifth pipeline; a fifth valve and a fifth delivery pump are arranged on the seventh pipeline; the bottom outlet of the waste liquid flash stripping tower is connected with the oil extraction tank area through a liquid discharge pipeline, and a sixth valve and a sixth delivery pump are arranged on the liquid discharge pipeline; and the drying tower is connected with the furfural storage tank through a seventh delivery pump.
Preferably, the degassing tower, the extraction tower, the evaporation tower, the waste liquid flash stripping tower and the drying tower are sequentially installed from left to right.
Preferably, the first line is connected to the extraction column at a position near the lower part of the extraction column, and the line between the eighth transfer pump and the extraction column is connected to the extraction column at a position near the upper part of the extraction column.
The utility model discloses owing to take above technical scheme, it has following advantage: 1. the utility model discloses a degasser, extraction tower, evaporation tower, waste liquid flash distillation strip tower, drying tower and waste liquid stove, the eighth delivery pump of bottom exit linkage of drying tower, the eighth delivery pump pass through three routes pipeline respectively with extraction tower, the first effect unit and two effect unit connection of evaporimeter, form three routes dry furfural line, can adjust the proportion of solvent and raw oil according to actual need, make the utility model discloses a different agent oil ratio products of device alternate production are showing the availability factor who improves the device, reduce the repetitive construction. 2. The utility model is provided with a seventh valve on the pipeline between the eighth delivery pump and the extraction tower; a second remote control valve and a second flowmeter are arranged on a pipeline between the eighth delivery pump and the first effect unit of the evaporator; a first remote control valve and a first flowmeter are arranged on a pipeline between the second-effect unit of the eighth delivery pump and the evaporator, so that the remote automatic operation of regulating the ratio of the agent to the oil is realized, the labor intensity is obviously reduced, and the production efficiency is improved.
Drawings
Fig. 1 is a schematic view of the overall structure of the present invention;
1. a degassing tower; 2. an extraction column; 3. an evaporation tower; 3A, a first effect unit; 3B, a double-effect unit; 3C, a triple effect unit; 4. a waste liquid flash stripping tower; 5. a drying tower; 6. a waste liquor furnace; 7. a first delivery pump; 8. a first valve; 9. a second valve; 10. a second delivery pump; 11. a third valve; 12. a first remote control valve; 13. a first flow meter; 14. a second remote control valve; 15. a second flow meter; 16. a fourth valve; 17. a fourth delivery pump; 18. a fifth valve; 19. a fifth delivery pump; 20. a sixth valve; 21. a sixth delivery pump; 22. a seventh delivery pump; 23. an eighth delivery pump; 24. a seventh valve; 25. a ninth delivery pump; 26. a second heat exchanger; 27. and an eighth valve.
Detailed Description
The preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings so that the objects, features and advantages of the invention can be more clearly understood. It should be understood that the embodiments shown in the drawings are not intended as limitations on the scope of the invention, but are merely illustrative of the true spirit of the technical solution of the invention.
As shown in fig. 1, the utility model provides a furfural refining device supporting wide solvent-oil ratio operating conditions, which comprises a degassing tower 1, an extraction tower 2, an evaporation tower 3, a waste liquid flash evaporation stripping tower 4, a drying tower 5 and a waste liquid furnace 6; the evaporation tower 3 is internally divided into a first-effect unit 3A, a third-effect unit 3C and a second-effect unit 3B from top to bottom;
the bottom outlet of the degassing tower 1 is connected with the extraction tower 2 through a first pipeline, and the top outlet of the degassing tower 1 discharges aldehyde-water mixed gas; the bottom outlet of the extraction tower 2 is connected with the first effect unit 3A of the evaporation tower 3 through a second pipeline, and the top outlet of the extraction tower 2 discharges refined oil; the top outlet of the first-effect unit 3A of the evaporation tower 3 is connected with the drying tower 5 through a third pipeline, the bottom outlet of the first-effect unit 3A of the evaporation tower 3 is connected with the second-effect unit 3B of the evaporation tower 3 through a fourth pipeline, the bottom outlet of the second-effect unit 3B of the evaporation tower 3 is connected with the waste liquid furnace 6 through a fifth pipeline, the waste liquid furnace 6 is connected with the third-effect unit 3C of the evaporation tower 3 through a sixth pipeline, and the bottom outlet of the third-effect unit 3C of the evaporation tower 3 is connected with the waste liquid flash evaporation stripping tower 4 through a seventh pipeline; the top outlet of the waste liquid flash evaporation stripping tower 4 is connected with the drying tower 5 through an eighth pipeline, and the bottom outlet of the waste liquid flash evaporation stripping tower 4 discharges extract oil; the top outlet of the drying tower 5 discharges aldehyde-water mixed gas, the bottom outlet of the drying tower 5 is connected with an eighth delivery pump 23, and the eighth delivery pump 23 is respectively connected with the extraction tower 2, the first-effect unit 3A and the second-effect unit 3B of the evaporator 3 through three pipelines.
In a preferred embodiment, a seventh valve 24 is provided in the line between the eighth transfer pump 23 and the extraction column 2; a second remote control valve 14 and a second flow meter 15 are provided on the line between the eighth delivery pump 23 and the primary unit 3A of the evaporator 3; a first remote control valve 12 and a first flow meter 13 are arranged on the line between the eighth delivery pump 23 and the two-effect unit 3B of the evaporator 3.
In a preferred embodiment, the degassing column 1 is connected to a feed line, on which a first feed pump 7 and a first valve 8 are arranged; a second valve 9 and a second delivery pump 10 are arranged on the first pipeline; a third valve 11 and a first heat exchanger (not shown in the figure) are arranged on the second pipeline; a ninth delivery pump 25, a second heat exchanger 26 and an eighth valve 27 are arranged on the fourth pipeline; a fourth valve 16 and a fourth delivery pump 17 are arranged on the fifth pipeline; a fifth valve 18 and a fifth delivery pump 19 are arranged on the seventh pipeline; the bottom outlet of the waste liquid flash evaporation stripping tower 4 is connected with the oil extraction tank area through a liquid drainage pipeline, and a sixth valve 20 and a sixth delivery pump 21 are arranged on the liquid drainage pipeline; the drying tower 5 is connected with a furfural storage tank through a seventh transfer pump 22.
In a preferred embodiment, the degassing tower 1, the extraction tower 2, the evaporation tower 3, the waste liquid flash evaporation stripping tower 4 and the drying tower 5 are sequentially installed from left to right, so that the layout of the whole device is optimized, the land utilization rate is improved, and the installation complexity of the device is reduced.
In a preferred embodiment, the first line is connected to the extraction column 2 at a position near the lower part of the extraction column 2, and the line between the eighth transfer pump 23 and the extraction column 2 is connected to the extraction column 2 at a position near the upper part of the extraction column 2, so that the extraction separation process can be realized by making both furfural and raw oil entering the extraction column 2 flow in the reverse direction.
The working process of the utility model is as follows:
the raw material enters a degassing tower 1 from a tank area after passing through a first conveying pump 7 and a first valve 8, the aldehyde-water mixed gas is discharged from a top outlet of the degassing tower 1, the rest part enters an extraction tower 2 through a second conveying pump 10 and a second valve 9 on a first pipeline and is mixed with recovered furfural sent from a drying tower 5, an extraction reaction is carried out in the extraction tower 2 to obtain an extract containing furfural and refined oil, the extract and the refined oil are separated into two phases in the extraction tower 2 according to different densities, and the refined oil is discharged from the top of the extraction tower 2 under self-pressure; the extract enters a second pipeline at the bottom of the extraction tower 2 through self-pressure, the extract is heated by a first heat exchanger and then is fed into a first effect unit 3A of an evaporation tower 3, part of aldehyde gas obtained by evaporation in the first effect unit 3A enters a drying tower 5, the rest mixed liquor in the first effect unit 3A is heated by a second heat exchanger 26 and is pumped into a second effect unit 3B by a ninth conveying pump 25, the mixed liquor in the second effect unit 3B is fed into a waste liquor furnace 6 through a fourth valve 16 and a fourth conveying pump 17, the mixture enters a third effect unit 3C in the evaporator 3 again after the temperature is increased, and the extract oil obtained by evaporation in the third effect unit 3C is fed into a waste liquor flash evaporation stripping tower 4 through a fifth valve 18 and a fifth conveying pump 19; the extracted oil enters a waste liquid flash evaporation stripping tower 4, secondary evaporation is carried out, after flash evaporation, the extracted oil is led out to an extracted oil tank area from the bottom, aldehyde gas is led out to a drying tower 5 from the top, the aldehyde gas in the drying tower 5 is mixed with wet furfural pumped in by a seventh conveying pump 22 to obtain dry furfural and aldehyde-water mixed gas, the aldehyde-water mixed gas is discharged from a top outlet of the drying tower 5, the dry furfural is discharged from a bottom outlet of the drying tower 5 and is divided into three paths after passing through an eighth conveying pump 23, and one path of the aldehyde-water mixed gas enters a primary effect unit 3A through a second remote control valve 14 and a second flow meter 15; one path enters a two-effect unit 3B through a first remote control valve 12 and a first flow meter 13, and the other path enters an eighth valve 24 and enters an extraction tower 2 to be used as recovered furfural to perform extraction reaction with raw oil entering the extraction tower 2.
When the agent-oil ratio needs to be switched according to actual production requirements, the opening degrees of the first remote control valve 12 and the second remote control valve 14 are adjusted to change the flow rate of furfural to the extraction tower 2, the first effect unit 3A and the second effect unit 3B, and the agent-oil ratio in the extraction tower 2 is changed, namely the switching of the agent-oil ratio is realized.
The following describes a specific process of switching the dosage-oil ratio by using the device of the present invention, with specific contents as follows:
adopt the utility model discloses a when the device carries out transformer base oil production, the raw materials is hydrogenation normal second line distillate oil, and the agent oil ratio is 2.5, furfural promptly: and (3) the raw oil is 2.5:1, 2.5 units of furfural and 1 unit of raw oil are injected into an extraction tower 2 at the moment, the produced extract oil contains 2.5 units of furfural and a plurality of raw oil components, and the quantity of the extract oil meets the requirement of subsequent heat transfer.
When the production of the rubber plasticizer needs to be switched, the solvent-oil ratio needs to be adjusted to 1.0, at the moment, the opening degrees of the first remote control valve 12 and the second remote control valve 14 are adjusted, so that the ratio of the furfural to the raw oil which is pumped into the extraction tower 2 is 1:1, and the furfural entering the first-effect unit 3A and the second-effect unit 3B of the evaporation tower 3 is 0.75 unit, therefore, even if the solvent-oil ratio is adjusted, the quantity of the produced extract oil is basically the same as that of the extract oil produced during the production of the transformer base oil, the subsequent heat balance of the whole device is maintained, and the normal operation of the whole device is ensured. Therefore, the whole device can alternately produce products with different oil ratios, the use efficiency of the device is greatly improved, the production cost is obviously reduced, and the economic benefit is greatly improved.
The present invention has been described only with reference to the above embodiments, and the structure, arrangement position and connection of the components may be changed. On the basis of the technical scheme of the utility model, the all sides according to the utility model discloses the principle is all not excluded to the improvement that individual part goes on or the transform of equivalence the utility model discloses a protection scope is outside.
Claims (5)
1. A furfural refining apparatus supporting wide solvent-oil ratio operating conditions, characterized in that:
comprises a degassing tower, an extraction tower, an evaporation tower, a waste liquid flash evaporation stripping tower, a drying tower and a waste liquid furnace; the evaporation tower is internally divided into a first-effect unit, a third-effect unit and a second-effect unit from top to bottom;
the bottom outlet of the degassing tower is connected with the extraction tower through a first pipeline, and the top outlet of the degassing tower discharges aldehyde-water mixed gas; the bottom outlet of the extraction tower is connected with the primary effect unit of the evaporation tower through a second pipeline, and the top outlet of the extraction tower discharges refined oil; the top outlet of the first-effect unit of the evaporation tower is connected with the drying tower through a third pipeline, the bottom outlet of the first-effect unit of the evaporation tower is connected with the second-effect unit of the evaporation tower through a fourth pipeline, the bottom outlet of the second-effect unit of the evaporation tower is connected with a waste liquid furnace through a fifth pipeline, the waste liquid furnace is connected with the third-effect unit of the evaporation tower through a sixth pipeline, and the bottom outlet of the third-effect unit of the evaporation tower is connected with the waste liquid flash evaporation stripping tower through a seventh pipeline; the top outlet of the waste liquid flash stripping tower is connected with the drying tower through an eighth pipeline, and the bottom outlet of the waste liquid flash stripping tower discharges extract oil; and an outlet at the top of the drying tower discharges aldehyde-water mixed gas, an outlet at the bottom of the drying tower is connected with an eighth delivery pump, and the eighth delivery pump is respectively connected with the extraction tower, the primary effect unit and the secondary effect unit of the evaporator through three pipelines.
2. A furfural refining plant supporting wide solvent oil ratio operating conditions according to claim 1 wherein:
a seventh valve is arranged on a pipeline between the eighth transfer pump and the extraction tower; a second remote control valve and a second flow meter are arranged on a pipeline between the eighth delivery pump and the primary effect unit of the evaporator; a first remote control valve and a first flow meter are provided on a line between the eighth transfer pump and the secondary effect unit of the evaporator.
3. A furfural refining plant supporting wide solvent oil ratio operating conditions according to claim 1 or 2 wherein:
the degassing tower is connected with a raw material conveying pipeline, and a first conveying pump and a first valve are arranged on the raw material conveying pipeline; a second valve and a second delivery pump are arranged on the first pipeline; a third valve and a first heat exchanger are arranged on the second pipeline; a ninth delivery pump, a second heat exchanger and an eighth valve are arranged on the fourth pipeline; a fourth valve and a fourth delivery pump are arranged on the fifth pipeline; a fifth valve and a fifth delivery pump are arranged on the seventh pipeline; the bottom outlet of the waste liquid flash stripping tower is connected with the oil extraction tank area through a liquid discharge pipeline, and a sixth valve and a sixth delivery pump are arranged on the liquid discharge pipeline; and the drying tower is connected with the furfural storage tank through a seventh delivery pump.
4. A furfural refining plant supporting wide solvent oil ratio operating conditions according to claim 1 or 2 wherein:
the degassing tower, the extraction tower, the evaporation tower, the waste liquid flash evaporation stripping tower and the drying tower are sequentially arranged from left to right.
5. A furfural refining plant supporting wide solvent oil ratio operating conditions according to claim 1 or 2 wherein:
the first line is connected to the extraction column at a position near the lower portion of the extraction column, and the line between the eighth transfer pump and the extraction column is connected to the extraction column at a position near the upper portion of the extraction column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020607826.5U CN212174844U (en) | 2020-04-21 | 2020-04-21 | Furfural refining device supporting wide solvent-oil ratio operation conditions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020607826.5U CN212174844U (en) | 2020-04-21 | 2020-04-21 | Furfural refining device supporting wide solvent-oil ratio operation conditions |
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| CN212174844U true CN212174844U (en) | 2020-12-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202020607826.5U Active CN212174844U (en) | 2020-04-21 | 2020-04-21 | Furfural refining device supporting wide solvent-oil ratio operation conditions |
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| Country | Link |
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| CN (1) | CN212174844U (en) |
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2020
- 2020-04-21 CN CN202020607826.5U patent/CN212174844U/en active Active
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