阅读说明：本技术 一种废润滑油、机油的精制再生工艺 (Refining regeneration process of waste lubricating oil and engine oil ) 是由 刘庆慧 薛强 薛金华 于 2021-09-28 设计创作，主要内容包括：本发明涉及废油再生技术领域,具体地说,涉及一种废润滑油、机油的精制再生工艺主要包括将废油过滤,再进行预处理得到废油污水、预处理原料油和轻质油,废油污水进行去污处理；将步骤一得到的预处理原料油馏分油得到150SN馏分油和350SN馏分油；将步骤二得到的150SN馏分油双溶剂萃取得到150SN产品油；将步骤二得到的350SN馏分油双溶剂萃取得到350SN产品油。该发明有效的提高了对废润滑油、机油的精制再生的利用率,同时有效降低了能源的利用,并且对废润滑油、机油的精制再生产生的附加材料能综合利用。(The invention relates to the technical field of waste oil regeneration, in particular to a refining and regenerating process of waste lubricating oil and engine oil, which mainly comprises the steps of filtering waste oil, pretreating to obtain waste oil sewage, pretreating raw oil and light oil, and decontaminating the waste oil sewage; obtaining 150SN distillate oil and 350SN distillate oil from the pretreated raw oil distillate oil obtained in the step one; extracting the 150SN distillate oil obtained in the step two by using a double solvent to obtain 150SN product oil; and (4) extracting the 350SN distillate oil obtained in the step (II) by using a double solvent to obtain 350SN product oil. The invention effectively improves the utilization rate of refining and regenerating the waste lubricating oil and the engine oil, simultaneously effectively reduces the utilization of energy, and can comprehensively utilize additional materials generated by refining and regenerating the waste lubricating oil and the engine oil.)

1. A refining and regenerating process of waste lubricating oil and engine oil is characterized in that: comprises the following steps:

the method comprises the following steps: filtering waste oil, pretreating to obtain waste oil sewage, pretreated raw oil and light oil, and decontaminating the waste oil sewage;

step two: obtaining 150SN distillate oil and 350SN distillate oil from the pretreated raw oil distillate oil obtained in the step one;

step three: extracting the 150SN distillate oil obtained in the step two by using a double solvent to obtain 150SN product oil;

step four: and (4) extracting the 350SN distillate oil obtained in the step (II) by using a double solvent to obtain 350SN product oil.

2. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the waste oil in the step one is specifically one of waste lubricating oil and waste engine oil.

3. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the pretreatment process in the first step is as follows:

s1: pressurizing and introducing waste oil into a raw material heat exchanger to exchange heat with circulating reflux liquid in a distillate oil recovery tower and heating;

s2: heating the waste oil subjected to heat exchange and temperature rise, and then feeding the waste oil into a flash tank to remove moisture, wherein the flash tank is controlled to be under negative pressure;

s3: and introducing the waste oil subjected to moisture removal into a light oil removal tower to remove light oil by vacuum heating, thereby obtaining pretreated raw oil and light oil.

4. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 3, characterized in that: the waste oil in the S2 and the light oil removal tower in the S3 are both electrically heated, and light oil is used as a heating source after the light oil is produced.

5. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the specific process of the distillate oil in the second step is that the pretreated raw oil is heated to 340 ℃ by a heating furnace and then is put into a distillate oil recovery tower for vacuum operation, 150SN distillate oil is extracted from the middle upper part of the distillate oil recovery tower, and 350SN distillate oil is extracted from the lower part of the distillate oil recovery tower.

6. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the 150SN distillate oil double-solvent extraction process in the third step is as follows:

l1: mixing 150SN distillate oil with a solvent, and introducing into a 150SN distillate oil preseparator for primary separation;

l2: buffering an upper layer material of a mixture of 150SN distillate oil and a solvent after primary separation in a 150SN distillate oil preseparator, introducing the buffered upper layer material into a 150SN distillate oil extraction tower, pressurizing a lower layer extract of the 150SN distillate oil preseparator, conveying the pressurized lower layer extract into a 150SN extract liquid cooler for cooling, introducing the cooled lower layer extract into a 150SN extract liquid separation tank for separation of the solvent and an oil phase, and introducing the oil phase and primary raffinate into the 150SN extraction tower;

l3: extracting impurities such as aromatic hydrocarbon, olefin and the like in distillate oil by a solvent at the lower part of a 150SN extraction tower, pressurizing and preheating an upper extract of the 150SN distillate oil extraction tower, then sending the extract into a solvent recovery tower for recovering a small amount of solvent, pumping the 150SN extract after recovering the solvent from the lower part of the solvent recovery tower, pressurizing, sending the 150SN extract into a 150SN stripping tower in an upper feeding mode for stripping, sending 150SN raffinate after stripping into a 150SN degassing tower for degassing and cooling to obtain 150SN product oil;

l4: one part of extract at the bottom of the 150SN extraction tower is sent to a 150SN distillate oil pre-separator, and the other part is sent to a regeneration tower for regeneration after light removal through a light removal tower, and is recycled.

7. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 6, characterized in that: the solvent in the L1 is specifically NMP and C9.

8. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the solvent recovery tower in the L3 is a lifting film evaporator structure, and the solvent recovered by the solvent recovery tower is sent to a separation tank to be recovered together with the solvent in the separation tank.

9. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the process of extracting 350SN distillate oil by using double solvents in the third step is as follows:

m1: sending 350SN distillate oil into a wiped film evaporator for separation to obtain residual oil and 350 oil phase;

m2: introducing 350SN oil phase extracted from the upper part of the wiped film evaporator into the lower part of a 350SN rectifying tower;

m3: putting the rectified 350 oil phase and a solvent into a 350SN pre-separator together for primary separation of the oil phase, taking out the primarily separated solvent from the lower part of the 350SN pre-separator, pressurizing and cooling the solvent, and introducing the solvent into a 150SN separation tank;

m4: sending 350SN primary raffinate at the upper part of the 350SN preseparator into a 350SN buffer tank, pumping the 350SN primary raffinate into a 350SN extraction tower to complete the extraction of the solvent on the impurities such as aromatic hydrocarbon, olefin and the like in 350SN distillate oil, and refluxing a part of extract at the bottom of the 350SN extraction tower to the 350SN preseparator after the extraction is completed;

m5: introducing the 350SN secondary raffinate extracted from the top of the 350SN preseparator into a buffer tank, pressurizing and preheating the buffer tank, and then introducing the buffer tank into a 350SN solvent recovery tower to recover a small amount of solvent in the 350SN secondary raffinate;

m6: and introducing the produced liquid at the lower part of the 350SN solvent recovery tower into a 350SN kettle liquid tank for pressurization, introducing into a 350SN stripping tower for stripping, degassing by a 350SN degassing tower, and recovering heat to obtain 350SN product oil.

10. The refining and regenerating process of the used lubricating oil and the engine oil according to claim 1, characterized in that: the solvent used in the 350SN distillate oil double-solvent extraction is specifically NMP and C9, the 350SN solvent recovery tower in the M5 is of a lifting film evaporator structure, and the recovered heat in the M6 is used for waste heat in the M5.

Technical Field

The invention relates to the technical field of waste oil regeneration, in particular to a refining regeneration process of waste lubricating oil and engine oil.

Background

The lubricating oil has various types, different characteristics and different purposes, but all the lubricating oil is gradually aged and deteriorated due to various pollution and physical and chemical actions in the using process, so that the lubricating oil needs to be replaced by new oil after being used for a certain period, and the replaced oil is waste mineral oil. The waste mineral oil belongs to organic petroleum hydrocarbon, is not degraded and toxic, so the pollution is large, if the waste mineral oil is abandoned or improperly disposed, resources are wasted, and the environment is greatly damaged. A large number of analytical tests and numerous production practices prove that the actual deteriorated components in the waste lubricating oil are not much and are mostly concentrated in polar compounds, the deteriorated components can be removed in the regeneration process, so that high-quality base oil can be produced, and the high-quality lubricating oil product can be produced by adopting the same additive formula as natural oil.

The existing process technology for refining base oil by circularly regenerating various waste lubricating oils as raw materials generally comprises a thin-film vacuum distillation and hydrofining technology, a sulfuric acid-clay technology, a topping distillation-acid-lime milk-clay technology and a pretreatment-distillation-furfural-clay technology. The thin film vacuum distillation and hydrofining technology has large investment, complex equipment technology, and poor practicability because of the need of higher-quality waste oil; the traditional sulfate clay technology has low yield, poor quality and serious secondary pollution, and is not allowed to be applied to a process for refining base oil by circularly regenerating waste lubricating oil serving as a raw material at present, so that a new process for refining base oil by circularly regenerating waste lubricating oil serving as a raw material is needed.

Disclosure of Invention

The invention aims to provide a refining and regenerating process of waste lubricating oil and engine oil, which aims to solve the problems in the background technology.

A refining and regenerating process of waste lubricating oil and engine oil comprises the following steps:

the method comprises the following steps: filtering waste oil, pretreating to obtain waste oil sewage, pretreated raw oil and light oil, and decontaminating the waste oil sewage;

step two: obtaining 150SN distillate oil and 350SN distillate oil from the pretreated raw oil distillate oil obtained in the step one;

step three: extracting the 150SN distillate oil obtained in the step two by using a double solvent to obtain 150SN product oil;

step four: and (4) extracting the 350SN distillate oil obtained in the step (II) by using a double solvent to obtain 350SN product oil.

Preferably, the waste oil in the first step is one of waste lubricating oil and waste engine oil.

As a further preferred, the pretreatment in step one comprises the following steps:

s1: pressurizing and introducing waste oil into a raw material heat exchanger to exchange heat with circulating reflux liquid in a distillate oil recovery tower and heating;

s2: heating the waste oil subjected to heat exchange and temperature rise, and then feeding the waste oil into a flash tank to remove moisture, wherein the flash tank is controlled to be under negative pressure;

s3: and introducing the waste oil subjected to moisture removal into a light oil removal tower to remove light oil by vacuum heating, thereby obtaining pretreated raw oil and light oil.

More preferably, the used oil in the S2 and the light oil removal tower in the S3 are both electrically heated, and light oil is used as a heating source after the light oil is produced.

Preferably, the distillate oil in the second step is prepared by heating the pretreated raw oil to 340 ℃ in a heating furnace, putting the pretreated raw oil into a distillate oil recovery tower for vacuum operation, extracting 150SN distillate oil from the middle upper part of the distillate oil recovery tower, and extracting 350SN distillate oil from the lower part of the distillate oil recovery tower.

As a further preference, the 150SN distillate oil double-solvent extraction process in the third step is as follows:

l1: mixing 150SN distillate oil with a solvent, and introducing into a 150SN distillate oil preseparator for primary separation;

l2: buffering an upper layer material of a mixture of 150SN distillate oil and a solvent after primary separation in a 150SN distillate oil preseparator, introducing the buffered upper layer material into a 150SN distillate oil extraction tower, pressurizing a lower layer extract of the 150SN distillate oil preseparator, conveying the pressurized lower layer extract into a 150SN extract liquid cooler for cooling, introducing the cooled lower layer extract into a 150SN extract liquid separation tank for separation of the solvent and an oil phase, and introducing the oil phase and primary raffinate into the 150SN extraction tower;

l3: extracting impurities such as aromatic hydrocarbon, olefin and the like in distillate oil by a solvent at the lower part of a 150SN extraction tower, pressurizing and preheating an upper extract of the 150SN distillate oil extraction tower, then sending the extract into a solvent recovery tower for recovering a small amount of solvent, pumping the 150SN extract after recovering the solvent from the lower part of the solvent recovery tower, pressurizing, sending the 150SN extract into a 150SN stripping tower in an upper feeding mode for stripping, sending 150SN raffinate after stripping into a 150SN degassing tower for degassing and cooling to obtain 150SN product oil;

l4: one part of extract at the bottom of the 150SN extraction tower is sent to a 150SN distillate oil pre-separator, and the other part is sent to a regeneration tower for regeneration after light removal through a light removal tower, and is recycled.

More preferably, the solvent in the L1 is specifically NMP and C9.

More preferably, the solvent recovery tower in the L3 is a falling film evaporator, and the solvent recovered by the solvent recovery tower is sent to the separation tank and is recovered together with the solvent in the separation tank.

As a further preference, the 350SN distillate oil double-solvent extraction process in the third step is as follows:

m1: sending 350SN distillate oil into a wiped film evaporator for separation to obtain residual oil and 350 oil phase;

m2: introducing 350SN oil phase extracted from the upper part of the wiped film evaporator into the lower part of a 350SN rectifying tower;

m3: putting the rectified 350 oil phase and a solvent into a 350SN pre-separator together for primary separation of the oil phase, taking out the primarily separated solvent from the lower part of the 350SN pre-separator, pressurizing and cooling the solvent, and introducing the solvent into a 150SN separation tank;

m4: sending 350SN primary raffinate at the upper part of the 350SN preseparator into a 350SN buffer tank, pumping the 350SN primary raffinate into a 350SN extraction tower to complete the extraction of the solvent on the impurities such as aromatic hydrocarbon, olefin and the like in 350SN distillate oil, and refluxing a part of extract at the bottom of the 350SN extraction tower to the 350SN preseparator after the extraction is completed;

m5: introducing the 350SN secondary raffinate extracted from the top of the 350SN preseparator into a buffer tank, pressurizing and preheating the buffer tank, and then introducing the buffer tank into a 350SN solvent recovery tower to recover a small amount of solvent in the 350SN secondary raffinate;

m6: and introducing the produced liquid at the lower part of the 350SN solvent recovery tower into a 350SN kettle liquid tank for pressurization, introducing into a 350SN stripping tower for stripping, degassing by a 350SN degassing tower, and recovering heat to obtain 350SN product oil.

More preferably, the solvent used in the 350SN distillate oil double-solvent extraction is specifically NMP and C9, and the 350SN solvent recovery tower in the M5 is of a lifting film evaporator structure.

As a further preference, the recovered heat in M6 is used for waste heat in M5.

Further preferably, the solvents used in the 150SN distillate two-solvent extraction and the 350SN distillate two-solvent extraction are the same and are used with each other.

Compared with the prior art, the invention has the beneficial effects that:

1. the quality of the regenerated base oil is excellent and can reach or approach the standard of natural petroleum base oil.

2. The light oil obtained by introducing the waste oil into the light oil removing tower and performing vacuum heating is used as a heating source, so that comprehensive utilization of energy is realized, and waste materials are not generated.

3. The product yield is high, 150SN distillate oil and 350SN distillate oil are obtained by oil separation, and the 150SN distillate oil and the 350SN distillate oil are respectively subjected to double-solvent extraction, so that the base oil component in the waste lubricating oil is fully utilized.

4. In the recycling of the double solvents, a double-effect evaporation technology is adopted, namely, a gas phase of a front-stage evaporator is used for providing a heat source for a lower-stage evaporator, and compared with the common one-effect evaporation, the double-effect evaporation method can save energy.

Drawings

FIG. 1 is a process flow diagram of the present invention;

FIG. 2 is a flow chart of a 150SN distillate oil double-solvent extraction process of the invention;

FIG. 3 is a flow chart of the 350SN distillate oil double-solvent extraction process of the invention.

Detailed Description

The invention discloses a refining and regenerating process of waste lubricating oil and engine oil, which is further detailed by specific embodiments.

The refining and regeneration process of the used lubricating oil and the engine oil of the embodiment comprises the following steps:

the method comprises the following steps: filtering waste oil, pretreating to obtain waste oil sewage, pretreated raw oil and light oil, and decontaminating the waste oil sewage;

step two: obtaining 150SN distillate oil and 350SN distillate oil from the pretreated raw oil distillate oil obtained in the step one;

step three: extracting the 150SN distillate oil obtained in the step two by using a double solvent to obtain 150SN product oil;

step four: and (4) extracting the 350SN distillate oil obtained in the step (II) by using a double solvent to obtain 350SN product oil.

Specifically, the waste oil in the step one is one of waste lubricating oil and waste engine oil.

In this embodiment, the pretreatment process in the first step is as follows:

s1: pressurizing and introducing waste oil into a raw material heat exchanger to exchange heat with circulating reflux liquid in a distillate oil recovery tower and heating;

s2: heating the waste oil subjected to heat exchange and temperature rise, and then feeding the waste oil into a flash tank to remove moisture, wherein the flash tank is controlled to be under negative pressure;

s3: and introducing the waste oil subjected to moisture removal into a light oil removal tower to remove light oil by vacuum heating, thereby obtaining pretreated raw oil and light oil.

Specifically, the waste oil in S2 and the light oil removal tower in S3 are both electrically heated, and light oil is used as a heating source after the light oil is produced.

And further, the specific process of the distillate oil in the step two is that the pretreated raw oil is heated to 340 ℃ through a heating furnace and then is put into a distillate oil recovery tower for vacuum operation, 150SN distillate oil is extracted from the middle upper part of the distillate oil recovery tower, and 350SN distillate oil is extracted from the lower part of the distillate oil recovery tower.

In this example, the two-solvent extraction process of 150SN distillate in step three is as follows:

l1: mixing 150SN distillate oil with a solvent, and introducing into a 150SN distillate oil preseparator for primary separation;

l2: buffering an upper layer material of a mixture of 150SN distillate oil and a solvent after primary separation in a 150SN distillate oil preseparator, introducing the buffered upper layer material into a 150SN distillate oil extraction tower, pressurizing a lower layer extract of the 150SN distillate oil preseparator, conveying the pressurized lower layer extract into a 150SN extract liquid cooler for cooling, introducing the cooled lower layer extract into a 150SN extract liquid separation tank for separation of the solvent and an oil phase, and introducing the oil phase and primary raffinate into the 150SN extraction tower;

l3: extracting impurities such as aromatic hydrocarbon, olefin and the like in distillate oil by a solvent at the lower part of a 150SN extraction tower, pressurizing and preheating an upper extract of the 150SN distillate oil extraction tower, then sending the extract into a solvent recovery tower for recovering a small amount of solvent, pumping the 150SN extract after recovering the solvent from the lower part of the solvent recovery tower, pressurizing, sending the 150SN extract into a 150SN stripping tower in an upper feeding mode for stripping, sending 150SN raffinate after stripping into a 150SN degassing tower for degassing and cooling to obtain 150SN product oil;

l4: one part of extract at the bottom of the 150SN extraction tower is sent to a 150SN distillate oil pre-separator, and the other part is sent to a regeneration tower for regeneration after light removal through a light removal tower, and is recycled.

Specifically, the solvent in L1 is specifically NMP and C9.

Further, the solvent recovery tower in the L3 is a falling film evaporator, and the solvent recovered by the solvent recovery tower is sent to the separation tank and recovered together with the solvent in the separation tank.

In this example, the 350SN distillate oil double-solvent extraction process in step three is as follows:

m1: sending 350SN distillate oil into a wiped film evaporator for separation to obtain residual oil and 350 oil phase;

m2: introducing 350SN oil phase extracted from the upper part of the wiped film evaporator into the lower part of a 350SN rectifying tower;

m3: putting the rectified 350 oil phase and a solvent into a 350SN pre-separator together for primary separation of the oil phase, taking out the primarily separated solvent from the lower part of the 350SN pre-separator, pressurizing and cooling the solvent, and introducing the solvent into a 150SN separation tank;

m4: sending 350SN primary raffinate at the upper part of the 350SN preseparator into a 350SN buffer tank, pumping the 350SN primary raffinate into a 350SN extraction tower to complete the extraction of the solvent on the impurities such as aromatic hydrocarbon, olefin and the like in 350SN distillate oil, and refluxing a part of extract at the bottom of the 350SN extraction tower to the 350SN preseparator after the extraction is completed;

m5: introducing the 350SN secondary raffinate extracted from the top of the 350SN preseparator into a buffer tank, pressurizing and preheating the buffer tank, and then introducing the buffer tank into a 350SN solvent recovery tower to recover a small amount of solvent in the 350SN secondary raffinate;

m6: and introducing the produced liquid at the lower part of the 350SN solvent recovery tower into a 350SN kettle liquid tank for pressurization, introducing into a 350SN stripping tower for stripping, degassing by a 350SN degassing tower, and recovering heat to obtain 350SN product oil.

Specifically, the solvent used in the 350SN distillate oil double-solvent extraction is NMP and C9, and the 350SN solvent recovery tower in M5 is a lifting film evaporator structure.

Further, the recovered heat in M6 is used for waste heat in M5.

The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and the preferred embodiments of the present invention are described in the above embodiments and the description, and are not intended to limit the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.