CN114686310B - Negative pressure desulfurization and low boiling device and application method thereof - Google Patents

Abstract

The application relates to the technical field of biodiesel desulfurization and low-boiling-point removal equipment, in particular to a negative pressure desulfurization and low-boiling-point removal device and a use method thereof. The negative pressure desulfurization and low boiling device comprises a flash tower, a plurality of desulfurization and low boiling components, an impurity reflux runner and a biodiesel reflux runner, wherein the desulfurization and low boiling components are arranged in the flash tower, and an inlet of the impurity reflux runner, a biodiesel outlet, an inlet of the biodiesel reflux runner and the impurity outlet are all led to the inside of the flash tower. The application has the effects of improving the removal rate of sulfur and low-boiling-point substances in the crude biodiesel and improving the purity of the biodiesel.

Description

Negative pressure desulfurization and low boiling device and application method thereof

Technical Field

The invention relates to the technical field of biodiesel desulfurization and low-boiling-point removal equipment, in particular to a negative pressure desulfurization and low-boiling-point removal device and a use method thereof.

Background

Biodiesel refers to fatty acid esters formed by ester conversion of biological oils such as vegetable oil, animal oil, waste oil, or microbial oil with methanol or ethanol. The biodiesel is a typical green energy source, and the great development of biodiesel has important strategic significance for sustainable development of economy, replacement of propulsion energy sources, alleviation of environmental pressure and control of urban atmospheric pollution.

However, the applicant found that, due to the relatively complex source of the bio-oil, elemental sulfur and some low boilers (C8, C10, C12, etc.) are likely to be generated during the process of preparing biodiesel. If the impurities such as sulfur, low-boiling substances and the like are not removed, the impurities can influence the color, smell and lightning of the biodiesel, so that the quality of the biodiesel is difficult to meet the national standard requirements of GB/T20828-2007 biodiesel (BD 100) for diesel fuel blending.

Although the skilled person can remove the sulfur and low-boiling-point substances by flash evaporation, the applicant believes that the heat exchange area of the biodiesel is relatively small due to the relatively small surface area of the tower plate in the flash evaporation tower, so that incomplete removal of the sulfur and low-boiling-point substances can be caused, and the produced biodiesel is unstable in quality, low in purity and limited in application.

Disclosure of Invention

In order to solve the problem that impurities such as sulfur, low-boiling substances and the like in crude biodiesel cannot be removed thoroughly, the application provides a negative pressure desulfurization and low-boiling removal device and a use method thereof.

In a first aspect, the application provides a negative pressure desulfurization and low boiling point removal device, which adopts the following technical scheme:

The negative pressure desulfurization and low-boiling-point removal device comprises a flash tower and a plurality of desulfurization and low-boiling-point removal components arranged in the flash tower, wherein the desulfurization and low-boiling-point removal components are sequentially and uniformly arranged at intervals along the height direction of the flash tower;

The desulfurization and low-boiling component comprises a liquid storage box and a heater fixedly connected with the liquid storage box, the liquid storage box is fixedly connected to the inner wall of the bottom of the flash evaporation tower, and the set temperature of the heater is between the boiling point of impurities and the boiling point of biodiesel;

The bottom of the flash evaporation tower is provided with a biodiesel liquid outlet pipe, the top of the flash evaporation tower is provided with an impurity air outlet pipe, the middle of the flash evaporation tower is provided with a crude biodiesel liquid inlet pipe, and the outlet of the crude biodiesel liquid inlet pipe faces into the liquid storage box positioned at the highest position;

The crude biodiesel liquid inlet pipe transfers the crude biodiesel into the liquid storage box at the highest position, and the crude biodiesel overflowed from the liquid storage box at the highest position is transferred into the liquid storage box below under the action of gravity.

Through adopting above-mentioned technical scheme, when need distill gas biodiesel, the staff can be at first with the settlement temperature of heater between impurity boiling point and biodiesel boiling point, later shift gas biodiesel to in the stock solution box of top through gas biodiesel feed pipe, the heater carries out continuous distillation to gas biodiesel to evaporate the impurity in the gas biodiesel upwards, and finally follow impurity outlet pipe row in.

With the addition of the crude biodiesel, the crude biodiesel in the highest liquid storage box gradually overflows, and the overflowed crude biodiesel is transferred into the liquid storage box below under the action of gravity for multiple distillation, and after the biodiesel is obtained by multiple distillation, the biodiesel directly flows out through a biodiesel liquid outlet pipe.

Compared with the conventional flash evaporation method in the background art, the flash evaporation method disclosed by the application has the advantages that the gas biodiesel is subjected to multiple distillation through the multi-layer liquid storage box, the heat exchange area and the heat exchange time of the biodiesel are indirectly increased, the removal rate of sulfur and low-boiling-point substances in the gas biodiesel is effectively improved, and the purity of the biodiesel is effectively improved.

Optionally, the desulfurization and low-boiling component further comprises a drainage plate fixedly connected to the bottom of the liquid storage box, and a drainage groove is formed in one side, close to the liquid storage box, of the drainage plate; the drainage plate gradually inclines downwards towards the direction close to the gas biodiesel liquid inlet pipe, the lower end of the drainage plate faces to the liquid storage box located below, and the upper end of the drainage plate is mutually spaced with the side wall of the flash evaporation tower.

Through adopting above-mentioned technical scheme, when the gas biodiesel in the stock solution box of highest department overflows gradually, the gas biodiesel that overflows shifts to on the drainage board at first, and the drainage board is through the drainage groove automatic with the gas biodiesel that overflows shift to the stock solution inslot of below as much as possible, effectively reduce the gas biodiesel that overflows directly through the possibility that the biodiesel drain pipe flows out, indirectly improve the purity degree of biodiesel.

Optionally, the flash distillation tower further comprises an impurity reflux runner, an impurity reflux pipe is arranged on the side wall of the flash distillation tower and positioned above the crude biodiesel liquid inlet pipe, an outlet of the impurity reflux pipe faces to the liquid storage box positioned at the highest position, an inlet of the impurity reflux runner is communicated with the impurity outlet pipe, and an outlet of the impurity reflux runner is communicated with the impurity reflux pipe.

Through adopting above-mentioned technical scheme, after impurity gas flows through impurity outlet duct, impurity reflux runner breaks away from impurity gas in the biodiesel of doping at first, then will break away from the biodiesel that obtains again and get into the flash column through impurity back flow and carry out the flash distillation in, effectively reduces the waste to biodiesel.

Optionally, the impurity reflux runner comprises a condenser, a reflux tank and an impurity tank which are sequentially connected, wherein a condensation inlet is formed in the upper end of the condenser, and the condensation inlet is communicated with the impurity outlet pipe; the lower end of the condenser is provided with a condensation outlet which is communicated with the reflux tank, and the set temperature of the condenser is between the boiling point of impurities and the boiling point of biodiesel;

A reflux cavity and an impurity discharging cavity which are communicated with each other are arranged in the reflux tank, a reflux inlet is arranged on the upper cavity wall of the reflux cavity, and the reflux inlet is communicated with the condensation outlet; the lower cavity wall of the reflux cavity is provided with a reflux outlet which is communicated with the impurity reflux pipe; the wall of the impurity discharging cavity is provided with an impurity outlet, and the impurity outlet is mutually communicated with the impurity tank.

Through adopting above-mentioned technical scheme, after impurity gas flows through impurity outlet duct, impurity gas changes at first and shifts to in the condenser, and the condenser condenses the partial biodiesel gas that mixes in the impurity gas, and the biodiesel that the subsequent condensation obtained directly gets into the backward flow intracavity to finally get into the flash column again through backward flow export and impurity back flow and distill, effectively reduce the waste to biodiesel.

Optionally, the impurity reflux flow channel further comprises a tail cooler, and the set temperature of the tail cooler is lower than the boiling point temperature of impurities; the impurity outlet set up in the lower chamber wall in impurity ejection of compact chamber, impurity ejection of compact chamber's upper chamber wall is provided with impurity liquefaction mouth, the lower extreme of tail cooler is provided with the cold entry of tail, the cold entry of tail with impurity liquefaction mouth intercommunication each other.

By adopting the technical scheme, the uncondensed impurity gas is gradually transferred into the tail cooler, the tail cooler condenses the impurity gas, and impurities obtained by condensation enter the impurity discharging cavity under the action of gravity and are finally transferred into the impurity tank through the impurity outlet. Compared with impurity gas, the impurity gas can be used for converting impurities into liquid, so that the operation difficulty of transferring and storing the impurities can be effectively reduced, and the impurity treatment efficiency can be indirectly improved.

Optionally, the device also comprises a biodiesel reflux flow passage, wherein the biodiesel reflux flow passage comprises a diverter and a rectification tower which are communicated with each other, and the diverter is used for separating impurities from biodiesel;

The flow divider is provided with a flow dividing inlet, a flow dividing impurity outlet and a flow dividing rectifying outlet, the biodiesel liquid outlet pipe is communicated with the flow dividing inlet, and the flow dividing rectifying outlet is communicated with the inlet of the rectifying tower; the side wall of flash column is provided with reposition of redundant personnel impurity back flow, reposition of redundant personnel impurity back flow export orientation in the receiver, reposition of redundant personnel impurity export with reposition of redundant personnel impurity back flow intercommunication each other.

Through adopting above-mentioned technical scheme, when biodiesel flows through the biodiesel drain pipe, biodiesel shifts to in the shunt at first, and the impurity liquid that mixes in the biodiesel is got rid of afterwards to finally shift to the flash column again through reposition of redundant personnel impurity export and reposition of redundant personnel impurity back flow and flash column in carrying out the flash distillation, effectively reduce the waste to biodiesel.

Optionally, a shunt cavity and a shunt impurity cavity which are mutually communicated are arranged in the shunt, a shunt heater is arranged at the lower part of the shunt cavity, and the set temperature of the shunt heater is between the boiling point of impurities and the boiling point of biodiesel; the upper part of the split flow cavity is provided with a split flow condenser, and the set temperature of the split flow condenser is less than the boiling point of impurities;

the utility model discloses a shunt impurity chamber, including shunt entry, shunt rectification export, shunt impurity outlet, shunt condenser, shunt entry and shunt rectification export set up in the chamber end in shunt impurity chamber, shunt impurity outlet set up in the chamber end in shunt impurity chamber, the lower terminal surface of shunt condenser is provided with the drainage face, the drainage face is close to the direction in shunt impurity chamber is downward sloping gradually, the lower extreme of drainage face orientation shunt impurity chamber.

By adopting the technical scheme, when the biodiesel flows out through the biodiesel liquid outlet pipe, the biodiesel is firstly transferred into the split flow cavity, and the split flow heater rectifies the biodiesel, so that impurities doped in the biodiesel are distilled out and transferred upwards; when impurity gas shifts to the shunt condenser department, the shunt condenser condenses impurity gas, and the impurity liquid that the condensation obtained then shifts to the reposition of redundant personnel impurity intracavity through the drainage face to finally get into the flash column again through reposition of redundant personnel impurity export and reposition of redundant personnel impurity back flow and distill, effectively reduce the waste to biodiesel.

Optionally, a partition plate is arranged in the split flow cavity, the partition plate divides the split flow cavity into a processing part and a discharging part, the split flow inlet and the split flow heater are both arranged in the processing part, and the split flow rectification outlet is arranged in the discharging part; the middle part of baffle runs through and has seted up the discharge gate, the biodiesel that overflows in the processing part shifts to in the discharge gate through the discharge gate.

By adopting the technical scheme, along with the addition of biodiesel in the treatment part, the rectified biodiesel is gradually upwards transferred, and when the rectified biodiesel is transferred to the discharge hole, the rectified biodiesel is firstly transferred to the discharge part through the discharge hole and finally transferred to the rectification removing tower through the split-flow rectification outlet, so that the purity of the biodiesel is indirectly improved.

In a second aspect, the application provides a method for using a negative pressure desulfurization and low-boiling device, which adopts the following technical scheme:

the application method of the negative pressure desulfurization and low boiling device comprises the following steps:

s1, adjusting the pressure in a flash tower to 1000Pa, adjusting the temperature in a liquid storage box to 200 ℃ through a heater, adjusting the temperature in a condenser to 180 ℃, and adjusting the temperature in a tail cooler to 25 ℃;

S2, transferring the crude biodiesel into an uppermost liquid storage box through a crude biodiesel liquid inlet pipe, and continuously distilling the crude biodiesel by a heater so as to evaporate impurities in the crude biodiesel upwards and finally discharging the impurities from an impurity gas outlet pipe row;

S3, transferring the impurity gas into a condenser, condensing part of biodiesel gas doped in the impurity gas by the condenser, directly entering a reflux cavity by the biodiesel obtained by condensation, and finally entering a flash tower again through a reflux outlet and an impurity reflux pipe for distillation;

The uncondensed impurity gas is gradually transferred into a tail cooler, the tail cooler condenses the impurity gas, and impurities obtained by condensation enter an impurity discharging cavity under the action of gravity and are finally transferred into an impurity tank through an impurity outlet;

s4, gradually overflowing the gas biodiesel in the liquid storage box at the highest position along with the addition of the gas biodiesel, and transferring the overflowed gas biodiesel into the liquid storage box below under the guidance of the drainage plate for multiple distillation; after the biodiesel is obtained through multiple times of distillation, the biodiesel directly flows out through a biodiesel liquid outlet pipe.

The application method of the negative pressure desulfurization and low boiling device comprises the following steps:

1. S1, adjusting the pressure in a flash tower to 1000Pa, adjusting the temperature in a liquid storage box to 200 ℃ through a heater, adjusting the temperature in a split-flow heater to 200 ℃, and adjusting the temperature in a split-flow condenser to 25 ℃;

2. Transferring the crude biodiesel into an uppermost liquid storage box through a crude biodiesel liquid inlet pipe, and continuously distilling the crude biodiesel by a heater so as to evaporate impurities in the crude biodiesel upwards and finally discharging the impurities from an impurity gas outlet pipe;

3. With the addition of the crude biodiesel, the crude biodiesel in the highest liquid storage box gradually overflows, and the overflowed crude biodiesel is transferred into the liquid storage box below under the guidance of the drainage plate for multiple distillation; after the biodiesel is obtained through multiple times of distillation, the biodiesel directly flows out through a biodiesel liquid outlet pipe;

4. The biodiesel enters the treatment part at first, and the split flow heater rectifies the biodiesel, so that impurities doped in the biodiesel are distilled out and transferred upwards; when the impurity gas is transferred to the shunt condenser, the shunt condenser condenses the impurity gas, the condensed impurity liquid is transferred to the shunt impurity cavity through the diversion surface, and finally enters the flash tower again through the shunt impurity outlet and the shunt impurity return pipe for distillation;

5. and with the addition of biodiesel in the treatment part, the rectified biodiesel is gradually transferred upwards, and when the rectified biodiesel is transferred to the discharge hole, the rectified biodiesel can be transferred to the discharge part through the discharge hole and finally transferred to the rectification removing tower through the split-flow rectification outlet.

In summary, the present application includes at least one of the following beneficial technical effects:

1. According to the flash evaporation method, the crude biodiesel is distilled for multiple times through the multi-layer liquid storage box, so that the heat exchange area and the heat exchange time of the biodiesel are indirectly increased, and the purity of the biodiesel is effectively improved;

2. when impurity gas flows out through an impurity outlet pipe, the impurity reflux flow channel firstly separates biodiesel doped in the impurity gas and enters the flash evaporation tower again for flash evaporation, so that the waste of the biodiesel is effectively reduced;

3. When the biodiesel flows out through the biodiesel liquid outlet pipe, the biodiesel is firstly transferred into the flow divider, and then the flow divider removes impurity liquid doped in the biodiesel and finally transfers the impurity liquid into the flash tower again for flash evaporation, so that the waste of the biodiesel is effectively reduced.

Drawings

FIG. 1 is a schematic flow diagram of a negative pressure desulfurization and low boiling point removal device.

FIG. 2 is a schematic flow diagram of a flash column and a desulfurization and de-low boiling assembly.

Fig. 3 is a flow chart of the impurity return flow channel.

Fig. 4 is a flow chart of the biodiesel return flow channel.

Reference numerals illustrate: 1. a flash column; 2. a desulfurization and low-boiling component; 3. impurity reflux flow channel; 4. a biodiesel return flow passage; 11. a crude biodiesel liquid inlet pipe; 12. an impurity outlet pipe; 13. an impurity return pipe; 14. a biodiesel liquid outlet pipe; 15. diverting an impurity return pipe; 21. a liquid storage box; 22. a heater; 23. a drainage plate; 24. drainage grooves; 31. a condenser; 32. a reflux drum; 33. a tail cooler; 34. an impurity tank; 41. a shunt; 42. removing the rectifying tower; 311. a condensing inlet; 312. a condensation outlet; 321. a reflow chamber; 322. an impurity discharging cavity; 331. a tail cooling inlet; 411. a shunt cavity; 412. a split impurity chamber; 413. a partition plate; 3211. a return inlet; 3212. a return outlet; 3221. an impurity liquefying port; 3222. an impurity outlet; 4111. a processing section; 4112. a discharging part; 4113. a split inlet; 4114. a split flow heater; 4115. a split condenser; 4116. a drainage surface; 4121. a split impurity outlet; 4131. a discharge port; 41121. and a split-flow rectification outlet.

Detailed Description

The application is described in further detail below with reference to fig. 1-4.

The embodiment of the application discloses a negative pressure desulfurization and low-boiling device. Referring to fig. 1, the negative pressure desulfurization and low boiling device comprises a flash evaporation tower 1, a plurality of desulfurization and low boiling components 2, an impurity reflux flow channel 3 and a biodiesel reflux flow channel 4, wherein the plurality of desulfurization and low boiling components 2 are all arranged in the flash evaporation tower 1, and an inlet and a biodiesel outlet of the impurity reflux flow channel 3 and an inlet and an impurity outlet 3222 of the biodiesel reflux flow channel 4 are all led to the inside of the flash evaporation tower 1.

When the flash evaporation operation is required to be carried out on the crude biodiesel, a worker can firstly fill the crude biodiesel into the desulfurization and low-boiling-point removal assemblies 2, and the plurality of desulfurization and low-boiling-point removal assemblies 2 carry out multiple times of distillation on the crude biodiesel, so that the crude biodiesel is converted into biodiesel and impurity gas consisting of sulfur and low-boiling-point substances.

The biodiesel is firstly transferred into the biodiesel reflux flow channel 4, the biodiesel reflux flow channel 4 removes impurity liquid doped in the biodiesel, and drives the impurity liquid to be transferred into the flash tower 1 again for secondary flash evaporation. The impurity gas is firstly transferred into the impurity reflux flow channel 3, the impurity reflux flow channel 3 removes the biodiesel doped in the impurity gas, and drives the biodiesel to be transferred into the flash tower 1 again in a liquid form for secondary flash evaporation.

Referring to fig. 1 and 2, taking the case that the desulfurization and denitrification low boiling components 2 are provided with four, the four desulfurization and denitrification low boiling components 2 are sequentially and uniformly arranged at intervals along the height direction of the flash tower 1. The middle part of the flash tower 1 is fixedly connected with a gas biodiesel liquid inlet pipe 11, and the outlet of the gas biodiesel liquid inlet pipe 11 faces into the desulfurization and low-boiling component 2 positioned at the highest position.

The desulfurization and denitrification low-boiling component 2 comprises a liquid storage box 21, a heater 22 and a drainage plate 23, wherein the liquid storage box 21 is fixedly connected to the inner wall of the flash evaporation tower 1, the heater 22 is fixedly connected to the liquid storage box 21, the drainage plate 23 is fixedly connected to the lower end face of the liquid storage box 21, and the outlet of the gas biodiesel liquid inlet pipe 11 faces the liquid storage box 21 located at the highest position.

In the present embodiment, the four heaters 22 are each temperature-controlled by adding heat transfer oil. In addition, in this embodiment, the drainage groove 24 is formed on the side of the drainage plate 23 close to the liquid storage box 21, and the drainage plate 23 gradually slopes downward toward the direction close to the biodiesel liquid inlet pipe. Wherein, the lower extreme of drainage board 23 is towards in the reservoir 21 that is located the below, and the upper end of drainage board 23 and the inner wall of flash column 1 interval each other.

When it is necessary to perform a flash operation on the crude biodiesel, the worker may first set the temperature in the liquid storage tank 21 to 200 ℃ and the pressure in the flash column 1 to 1000Pa by the heater 22, and then fill the crude biodiesel into the highest liquid storage tank 21 by the worker through the crude biodiesel feed pipe 11.

At this time, since the boiling point of the low boiling point substance is 170 ℃ and the boiling point of sulfur is between 160 and 170 ℃, the heater 22 can distill out the low boiling point substance and sulfur and other impurities in the crude biodiesel, and the biodiesel is stored in the liquid storage box 21. Since the upper end of the flow-guiding plate 23 is spaced from the inner wall of the flash column 1, the flow-guiding plate 23 itself is unlikely to hinder the rise of the impurity gas.

Along with the addition of the crude biodiesel, the biodiesel in the liquid storage box 21 positioned at the highest position gradually overflows, at the moment, the overflowed biodiesel gradually permeates through the light-resistant drainage plates 23 and is transferred into the liquid storage box 21 below to be distilled for a plurality of times, the distilled impurity gas continues to be transferred upwards through the gap between the drainage plates 23 and the inner wall of the flash tower 1, and the biodiesel gradually transfers downwards.

Referring to fig. 2 and 3, an impurity outlet pipe 12 and an impurity return pipe 13 are fixedly connected to the top of the flash distillation column 1, an inlet of the impurity return flow channel 3 is communicated with the impurity outlet pipe 12, and an outlet of the impurity return flow channel 3 is communicated with the impurity return pipe 13. The impurity return pipe 13 is located above the gas biodiesel inlet pipe 11, and the outlet of the impurity return pipe 13 is directed into the liquid storage box 21 located at the highest position.

Specifically, the impurity reflux passage 3 includes a condenser 31, a reflux drum 32, a tail cooler 33, and an impurity drum 34, which are connected in this order. Wherein, the upper end of the condenser 31 is provided with a condensation inlet 311, the lower end of the condenser 31 is provided with a condensation outlet 312, the condensation inlet 311 is communicated with the impurity outlet, and the condensation outlet 312 is communicated with the reflux drum 32. In the present embodiment, the set temperature in the condenser 31 is 180 ℃, and the temperature is controlled by the heat transfer oil.

A reflux cavity 321 and an impurity discharging cavity 322 which are mutually communicated are arranged in the reflux tank 32, wherein a reflux inlet 3211 is formed in the upper cavity wall of the reflux cavity 321, a reflux outlet 3212 is formed in the lower cavity wall of the reflux cavity 321, the reflux inlet 3211 is mutually communicated with the condensation outlet 312, and the reflux outlet 3212 is mutually communicated with the impurity reflux pipe 13. Impurity liquefaction opening 3221 has been seted up to impurity ejection of compact chamber 322's upper chamber wall, and impurity export 3222 has been seted up to impurity ejection of compact chamber 322's lower chamber wall, and tail cooler 33 and impurity liquefaction opening 3221 communicate each other, and impurity export 3222 and impurity jar 34 communicate each other.

The tail cooler 33 has a tail cooling inlet 331 formed at a lower end thereof, and the tail cooling inlet 331 is communicated with the impurity liquefying inlet 3221. In the present embodiment, the set temperature of the tail cooler 33 is 25 ℃, and the temperature is controlled by cooling water.

When the impurity gas needs to be separated and refluxed, the worker can transfer the impurity gas into the condenser 31 through the impurity outlet pipe 12, at this time, since the temperature in the condenser 31 is between the boiling point of the biodiesel and the boiling point of the impurity, the biodiesel is gradually liquefied and automatically transferred into the reflux cavity 321 under the action of gravity, and then the biodiesel is driven to flow through the reflux outlet 3212 and the impurity reflux port through the reflux pump, and finally enters the flash tower 1 for distillation.

The uncondensed impurity gas is transferred to the tail cooler 33 by the suction pump, and the impurity gas is gradually liquefied and automatically transferred to the impurity discharging cavity 322 because the temperature in the tail cooler 33 is lower than the boiling point of the impurity, and then transferred to the impurity tank 34 through the impurity outlet 3222 and the discharging pump.

Referring to fig. 2 and 4, the bottom of the flash tower 1 is fixedly connected with a biodiesel liquid outlet pipe 14, the middle of the flash tower 1 is fixedly connected with a diversion impurity return pipe 15, and the outlet of the diversion impurity return pipe 15 faces into a second liquid storage box 21 from bottom to top. The inlet of the biodiesel reflux flow passage 4 is communicated with the biodiesel liquid outlet pipe 14, and the impurity outlet 3222 of the biodiesel reflux flow passage 4 is communicated with the shunt impurity reflux pipe 15.

Specifically, the biodiesel reflux runner 4 includes a splitter 41 and a rectifying tower 42 that are mutually communicated, wherein a splitting cavity 411 and a splitting impurity cavity 412 that are mutually communicated are disposed in the splitter 41, a partition 413 is fixedly connected in the splitting cavity 411, and the partition 413 divides the splitting cavity 411 into a processing portion 4111 and a discharging portion 4112.

The bottom of the treatment portion 4111 is provided with a split inlet 4113, the bottom of the split impurity chamber 412 is provided with a split impurity outlet 4121, the split inlet 4113 is communicated with the biodiesel liquid outlet pipe 14, and the split impurity outlet 4121 is communicated with the split impurity return pipe 15. The split flow heater 4114 is fixedly connected to the bottom of the processing portion 4111, and the split flow condenser 4115 is fixedly connected to the top of the processing portion 4111.

Wherein, the setting temperature of the split heater 4114 is 200 ℃, and the temperature of the split heater 4114 is controlled by the heat transfer oil. The set temperature of the split condenser 4115 is 25 ℃, and the temperature of the split condenser 4115 is controlled by the cooling water. In the present embodiment, the lower end surface of the split-flow condenser 4115 is provided with a drainage surface 4116, the drainage surface 4116 gradually slopes downward toward the split-flow impurity chamber 412, and the lower end of the drainage surface 4116 faces the split-flow impurity chamber 412.

When the biodiesel flows out through the biodiesel outlet pipe 14, the biodiesel is first transferred into the treatment section 4111 through the split inlet 4113, and at this time, the split heater 4114 distills the biodiesel, thereby evaporating and transferring upward impurities remaining in the biodiesel. When the impurity gas is transferred to the split condenser 4115, the split condenser 4115 converts the impurity gas into a liquid state, and finally transfers the liquid state to the split impurity chamber 412 through the drainage surface 4116, and then drives the impurity to flow through the split impurity outlet 4121 and the split impurity return pipe 15 through the bottom pump, and finally transfers the impurity gas to the flash tower 1 for distillation.

The middle part of the baffle 413 is provided with a discharge hole 4131 in a penetrating way, the bottom of the discharge cavity is provided with a split-flow rectifying outlet 41121, and the split-flow rectifying outlet 41121 is communicated with the rectifying tower 42. With the addition of biodiesel in the treatment section 4111, the rectified biodiesel is gradually transferred upwards, and when the rectified biodiesel is transferred to the discharge hole, the rectified biodiesel is transferred to the discharge section 4112 through the discharge hole first, and finally transferred to the rectification tower 42 through the split-flow rectification outlet 41121.

In this embodiment, the flow channels and the flash tower 1 are all connected by pipes, and the fixed connection may be a conventional fixed connection manner such as welding, integral molding, or bolting.

The embodiment of the application discloses a use method of a negative pressure desulfurization and low boiling point removal device, which comprises the following steps:

s1, adjusting the pressure in the flash tower 1 to 1000Pa, adjusting the temperature in the liquid storage box 21 to 200 ℃ through the heater 22, adjusting the temperature in the condenser 31 to 180 ℃ and adjusting the temperature in the tail cooler 33 to 25 ℃; the temperature in the split heater 4114 was adjusted to 200℃and the temperature in the split condenser 4115 was adjusted to 25℃respectively

S2, transferring the crude biodiesel into an uppermost liquid storage box 21 through a crude biodiesel liquid inlet pipe 11, and continuously distilling the crude biodiesel by a heater 22 so as to evaporate impurities in the crude biodiesel upwards and finally discharging the impurities from an impurity outlet pipe 12;

S3, transferring the impurity gas into a condenser 31, condensing part of biodiesel gas doped in the impurity gas by the condenser 31, directly entering a reflux cavity 321 by the biodiesel obtained by condensation, and finally entering the flash tower 1 again through a reflux outlet 3212 and an impurity reflux pipe 13 for distillation;

The uncondensed impurity gas is gradually transferred into the tail cooler 33, the tail cooler 33 condenses the impurity gas, and the condensed impurity enters the impurity discharging cavity 322 under the action of gravity and is finally transferred into the impurity tank 34 through the impurity outlet 3222;

S4, along with the addition of the biodiesel, the biodiesel in the highest liquid storage box 21 gradually overflows, and the overflowed biodiesel is transferred into the liquid storage box 21 below under the guidance of the drainage plate 23 for multiple distillation; after the biodiesel is obtained through multiple times of distillation, the biodiesel directly flows out through the biodiesel liquid outlet pipe 14;

s5, the biodiesel enters the treatment part 4111 at first, and the split flow heater 4114 rectifies the biodiesel, so that impurities doped in the biodiesel are distilled out and transferred upwards; when the impurity gas is transferred to the split condenser 4115, the split condenser 4115 condenses the impurity gas, and the condensed impurity liquid is transferred to the split impurity chamber 412 through the drainage surface 4116, and finally enters the flash tower 1 again through the split impurity outlet 4121 and the split impurity return pipe 15 for distillation;

s6, with the addition of biodiesel in the treatment portion 4111, the rectified biodiesel is gradually transferred upwards, and when the rectified biodiesel is transferred to the discharge hole, the rectified biodiesel can be transferred to the discharge portion 4112 through the discharge hole and finally transferred to the rectification tower 42 through the split-flow rectification outlet 41121.

The above embodiments are not intended to limit the scope of the present application, so: all equivalent changes in structure, shape and principle of the application should be covered in the scope of protection of the application.

Claims (7)

1. A negative pressure desulfurization and low boiling device is characterized in that: the device comprises a flash evaporation tower (1) and a plurality of desulfurization and low-boiling-point removal components (2) arranged in the flash evaporation tower (1), wherein the desulfurization and low-boiling-point removal components (2) are sequentially and uniformly arranged at intervals along the height direction of the flash evaporation tower (1);

the desulfurization and low-boiling-point removal component (2) comprises a liquid storage box (21) and a heater (22) fixedly connected with the inside of the liquid storage box (21), the liquid storage box (21) is fixedly connected to the inner wall of the bottom of the flash evaporation tower (1), and the set temperature of the heater (22) is between the boiling point of impurities and the boiling point of biodiesel;

The bottom of the flash evaporation tower (1) is provided with a biodiesel liquid outlet pipe (14), the top of the flash evaporation tower (1) is provided with an impurity air outlet pipe (12), the middle part of the flash evaporation tower (1) is provided with a crude biodiesel liquid inlet pipe (11), and the outlet of the crude biodiesel liquid inlet pipe (11) faces into the liquid storage box (21) positioned at the highest position;

The crude biodiesel liquid inlet pipe (11) transfers the crude biodiesel into the liquid storage box (21) positioned at the highest position, and the crude biodiesel overflowed from the liquid storage box (21) positioned at the highest position is transferred into the liquid storage box (21) below under the action of gravity;

The desulfurization and low-boiling-point removal assembly (2) further comprises a drainage plate (23) fixedly connected to the bottom of the liquid storage box (21), and a drainage groove (24) is formed in one side, close to the liquid storage box (21), of the drainage plate (23); the drainage plate (23) gradually inclines downwards towards the direction close to the crude biodiesel liquid inlet pipe (11), the lower end of the drainage plate (23) faces into the liquid storage box (21) positioned below, and the upper end of the drainage plate (23) is mutually spaced from the side wall of the flash tower (1);

The flash distillation tower further comprises an impurity reflux flow channel (3), an impurity reflux pipe (13) is arranged on the side wall of the flash distillation tower (1), the impurity reflux pipe (13) is positioned above the crude biodiesel liquid inlet pipe (11), the outlet of the impurity reflux pipe (13) faces into the liquid storage box (21) positioned at the highest position, the inlet of the impurity reflux flow channel (3) is communicated with the impurity outlet pipe (12), and the outlet of the impurity reflux flow channel (3) is communicated with the impurity reflux pipe (13);

The impurity reflux runner (3) comprises a condenser (31), a reflux tank (32) and an impurity tank (34) which are sequentially connected, a condensation inlet (311) is formed in the upper end of the condenser (31), and the condensation inlet (311) is communicated with the impurity outlet pipe (12); the lower end of the condenser (31) is provided with a condensation outlet (312), the condensation outlet (312) is communicated with the reflux tank (32), and the set temperature of the condenser (31) is between the boiling point of impurities and the boiling point of biodiesel;

a reflux cavity (321) and an impurity discharging cavity (322) which are mutually communicated are arranged in the reflux tank (32), a reflux inlet (3211) is arranged on the upper cavity wall of the reflux cavity (321), and the reflux inlet (3211) is mutually communicated with the condensation outlet (312); the lower cavity wall of the reflux cavity (321) is provided with a reflux outlet (3212), and the reflux outlet (3212) is communicated with the impurity reflux pipe (13); the wall of the impurity discharging cavity (322) is provided with an impurity outlet (3222), and the impurity outlet (3222) is communicated with the impurity tank (34).

2. The negative pressure desulfurization and low boiling device according to claim 1, wherein: the impurity reflux flow channel (3) further comprises a tail cooler (33), and the set temperature of the tail cooler (33) is lower than the boiling point temperature of impurities; the impurity outlet (3222) set up in the lower chamber wall of impurity ejection of compact chamber (322), the upper chamber wall of impurity ejection of compact chamber (322) is provided with impurity liquefaction mouth (3221), the lower extreme of tail cooler (33) is provided with tail cold entry (331), tail cold entry (331) with impurity liquefaction mouth (3221) intercommunication each other.

3. The negative pressure desulfurization and low boiling device according to claim 1, wherein: the device further comprises a biodiesel reflux flow channel (4), wherein the biodiesel reflux flow channel (4) comprises a flow divider (41) and a rectification column (42) which are communicated with each other, and the flow divider (41) is used for separating impurities from biodiesel;

The splitter (41) is provided with a splitting inlet (4113), a splitting impurity outlet (4121) and a splitting rectification outlet (41121), the biodiesel liquid outlet pipe (14) is communicated with the splitting inlet (4113), and the splitting rectification outlet (41121) is communicated with the inlet of the rectification removing tower (42); the side wall of flash column (1) is provided with reposition of redundant personnel impurity back flow (15), the export orientation of reposition of redundant personnel impurity back flow (15) in receiver (21), reposition of redundant personnel impurity export (4121) with reposition of redundant personnel impurity back flow (15) intercommunication each other.

4. The negative pressure desulfurization and low boiling device according to claim 3, wherein: a diversion cavity (411) and a diversion impurity cavity (412) which are mutually communicated are arranged in the diverter (41), a diversion heater (4114) is arranged at the lower part of the diversion cavity (411), and the set temperature of the diversion heater (4114) is between the boiling point of impurities and the boiling point of biodiesel; a split condenser (4115) is arranged at the upper part of the split cavity (411), and the set temperature of the split condenser (4115) is less than the boiling point of impurities;

The utility model discloses a shunt impurity separation device, including shunt entry (4113) and shunt rectification export (41121), shunt impurity export (4121) set up in shunt impurity chamber (412)'s chamber end, shunt condenser (4115)'s lower terminal surface is provided with drainage face (4116), drainage face (4116) to be close to the direction of shunt impurity chamber (412) slopes downwards gradually, the lower extreme of drainage face (4116) is towards shunt impurity chamber (412).

5. The negative pressure desulfurization and denitrification low boiling device according to claim 4, wherein: a partition plate (413) is arranged in the diversion cavity (411), the partition plate (413) divides the diversion cavity (411) into a processing part (4111) and a discharging part (4112), the diversion inlet (4113) and the diversion heater (4114) are both arranged in the processing part (4111), and the diversion rectification outlet (41121) is arranged in the discharging part (4112); the middle part of the baffle (413) is provided with a discharge hole in a penetrating way, and the biodiesel overflowed from the treatment part (4111) is transferred into the discharge part (4112) through the discharge hole.

6. A method of using the negative pressure desulfurization and low boiling point removal device of claim 1, comprising the steps of:

S1, adjusting the pressure in a flash tower (1) to 1000Pa, adjusting the temperature in a liquid storage box (21) to 200 ℃ through a heater (22), adjusting the temperature in a condenser (31) to 180 ℃ and adjusting the temperature in a tail cooler (33) to 25 ℃;

s2, transferring the crude biodiesel into an uppermost liquid storage box (21) through a crude biodiesel liquid inlet pipe (11), and continuously distilling the crude biodiesel by a heater (22), so that impurities in the crude biodiesel are distilled upwards and finally discharged from an impurity outlet pipe (12);

S3, transferring the impurity gas into a condenser (31), condensing part of biodiesel gas doped in the impurity gas by the condenser (31), directly entering a reflux cavity (321) by the biodiesel obtained by condensation, and finally entering a flash tower (1) again through a reflux outlet (3212) and an impurity reflux pipe (13) for distillation;

The uncondensed impurity gas is gradually transferred into a tail cooler (33), the tail cooler (33) condenses the impurity gas, and impurities obtained by condensation enter an impurity discharging cavity (322) under the action of gravity and are finally transferred into an impurity tank (34) through an impurity outlet (3222);

S4, gradually overflowing the gas biodiesel in the liquid storage box (21) at the highest position along with the addition of the gas biodiesel, and transferring the overflowed gas biodiesel into the liquid storage box (21) below under the guidance of the drainage plate (23) for multiple distillation; after the biodiesel is obtained by multiple times of distillation, the biodiesel directly flows out through a biodiesel liquid outlet pipe (14).

7. A method of using the negative pressure desulfurization and low boiling point removal device as claimed in claim 5, comprising the steps of:

s1, adjusting the pressure in a flash tower (1) to 1000Pa, adjusting the temperature in a liquid storage box (21) to 200 ℃ through a heater (22), adjusting the temperature in a split-flow heater (4114) to 200 ℃, and adjusting the temperature in a split-flow condenser (4115) to 25 ℃;

S2, transferring the crude biodiesel into an uppermost liquid storage box (21) through a crude biodiesel liquid inlet pipe (11), and continuously distilling the crude biodiesel by a heater (22), so that impurities in the crude biodiesel are distilled upwards and finally discharged from an impurity outlet pipe (12);

S3, gradually overflowing the gas biodiesel in the liquid storage box (21) at the highest position along with the addition of the gas biodiesel, and transferring the overflowed gas biodiesel into the liquid storage box (21) below under the guidance of the drainage plate (23) for multiple distillation; after the biodiesel is obtained through multiple times of distillation, the biodiesel directly flows out through a biodiesel liquid outlet pipe (14);

S4, the biodiesel enters a treatment part (4111) at first, and the split flow heater (4114) rectifies the biodiesel, so that impurities doped in the biodiesel are steamed out and transferred upwards; when the impurity gas is transferred to the split condenser (4115), the split condenser (4115) condenses the impurity gas, and the condensed impurity liquid is transferred into the split impurity cavity (412) through the diversion surface (4116) and finally enters the flash tower (1) again through the split impurity outlet (4121) and the split impurity return pipe (15) for distillation;

S5, along with the addition of biodiesel in the treatment part (4111), the rectified biodiesel is gradually transferred upwards, and when the rectified biodiesel is transferred to the discharge hole, the rectified biodiesel can be transferred into the discharge part (4112) through the discharge hole and finally transferred into the rectification tower (42) through the split-flow rectification outlet (41121).