CN113698959A - Waste mineral oil recovery treatment process - Google Patents
Waste mineral oil recovery treatment process Download PDFInfo
- Publication number
- CN113698959A CN113698959A CN202111140487.XA CN202111140487A CN113698959A CN 113698959 A CN113698959 A CN 113698959A CN 202111140487 A CN202111140487 A CN 202111140487A CN 113698959 A CN113698959 A CN 113698959A
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- Prior art keywords
- oil
- waste mineral
- mineral oil
- tank
- rectifying tower
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- 239000002699 waste material Substances 0.000 title claims abstract description 74
- 239000002480 mineral oil Substances 0.000 title claims abstract description 66
- 235000010446 mineral oil Nutrition 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000011084 recovery Methods 0.000 title claims description 11
- 239000003921 oil Substances 0.000 claims abstract description 67
- 239000012071 phase Substances 0.000 claims abstract description 23
- 238000002156 mixing Methods 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 238000005189 flocculation Methods 0.000 claims abstract description 14
- 230000016615 flocculation Effects 0.000 claims abstract description 14
- 238000004821 distillation Methods 0.000 claims abstract description 8
- 238000005086 pumping Methods 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims abstract description 8
- 239000007787 solid Substances 0.000 claims abstract description 6
- 239000007791 liquid phase Substances 0.000 claims abstract description 5
- 239000002199 base oil Substances 0.000 claims description 33
- 238000003860 storage Methods 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000007670 refining Methods 0.000 claims description 9
- 239000008394 flocculating agent Substances 0.000 claims description 8
- 239000000839 emulsion Substances 0.000 claims description 7
- 238000001704 evaporation Methods 0.000 claims description 7
- 230000008020 evaporation Effects 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000005119 centrifugation Methods 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 11
- 239000004927 clay Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 239000010913 used oil Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
Abstract
The invention discloses a process for recovering and treating waste mineral oil, which comprises the following steps of a, detecting the solid content of the waste mineral oil; b, putting the high-solid-content waste mineral oil in the step a into a flocculation blending tank; c, blending the waste mineral oil by a flocculation blending tank, and then feeding the waste mineral oil into a three-phase separator, and feeding the waste mineral oil into an intermediate tank; d, adding a small amount of flocculant into the intermediate tank, continuously stirring, and performing a reduced pressure distillation process; e, enabling the waste mineral oil in the intermediate tank to enter a first-stage evaporator, enabling a liquid phase to enter a second-stage evaporator, pumping liquid oil at the bottom of the second-stage evaporator into a scraper evaporator, and enabling a gas phase to directly enter a rectifying tower; f, carrying out reduced pressure distillation in the rectifying tower; and g, treating with argil to obtain a finished product. The rectification process of the rectification tower realizes the recutting of the waste mineral oil fraction, and has safe process steps, less environmental pollution and higher yield.
Description
Technical Field
The invention relates to the technical field of waste mineral oil treatment, in particular to a waste mineral oil recovery treatment process.
Background
The polluting nature and availability of used oils require careful treatment in our industrial production, which can cause environmental pollution if not properly treated and can also cause industrial hazards if not technically treated.
The traditional waste mineral oil recovery and regeneration technology comprises a distillation-sulfuric acid-clay refining process, but the process has a large influence on environmental pollution, a solvent refining process has a high cost, and a hydrofining process has certain dangers, so that the existing waste mineral oil treatment process needs to be further improved.
Disclosure of Invention
The present invention is directed to overcoming the above-mentioned deficiencies in the art and providing an improved and more flexible process for the recovery and treatment of waste mineral oil.
In order to achieve the purpose, the invention discloses a waste mineral oil recovery treatment process, which adopts the following technical scheme.
A process for recovering and treating waste mineral oil includes such steps as,
a, detecting solid content of waste mineral oil, dividing the waste mineral oil into low-solid-content waste mineral oil and high-solid-content waste mineral oil, putting the low-solid-content waste mineral oil into a filtering structure with a grating, and enabling the low-solid-content waste mineral oil to enter a raw material storage oil tank after passing through the filtering structure;
b, putting the high-solid-content waste mineral oil in the step a into a flocculation blending tank;
c, blending the waste mineral oil through a flocculation blending tank, then feeding the waste mineral oil into a three-phase separator, separating out a flocculating agent, oil residues and the waste mineral oil, feeding the waste mineral oil into an intermediate tank, directly feeding the waste mineral oil with low solid content in a raw oil storage tank into a flocculation tank, not adding the flocculating agent, separating out the water through three-phase centrifugation, feeding the oil phase into a raw oil storage tank, mixing the oil phase with other waste mineral oil, then performing the circulation of the step b, and directly feeding the water phase into an emulsion workshop for treatment;
d, adding a small amount of flocculant into the intermediate tank, continuously stirring, and performing a reduced pressure distillation process;
e, enabling the waste mineral oil in the intermediate tank to enter a first-stage evaporator, pumping a distilled water-oil mixture into an oil-water separation tank through a pipeline after secondary condensation, enabling a liquid phase to enter a second-stage evaporator, pumping liquid oil at the bottom of the second-stage evaporator into a scraper evaporator, directly enabling a gas phase to enter a rectifying tower, gasifying the liquid oil in the scraper evaporator, introducing the gas phase into the rectifying tower from the top of the scraper evaporator by vacuum, removing residual oil by a scraper, enabling the residual oil to enter a bottom oil residue receiving tank, and pumping the residual oil into an oil residue storage tank;
f, carrying out reduced pressure distillation in the rectifying tower, controlling the temperature at the top of the rectifying tower to be 170-200 ℃, and under the condition that the vacuum degree is about-0.098 MPa (40mmHg), taking the fraction at the top of the rectifying tower as a first-line base oil gas, condensing and recovering the first-line base oil gas, and then, controlling the temperature to be about 40 ℃, and receiving the first-line base oil gas by an overhead oil storage tank to obtain first-line base oil; controlling the temperature of the rectifying tower to be 250-270 ℃, and flowing the required liquid oil into a second-line receiving tank under the condition that the vacuum degree is about 30mmHg, and flowing the high-temperature difference into a first refining stripping tank; controlling the temperature of the rectifying tower to be 290-310 ℃, and flowing the required liquid oil into a three-line receiving tank under the condition of a vacuum degree of about 30mmHg, and flowing the high-temperature difference into a second refining stripping tank; residual liquid of the remaining heavy components is tower bottom oil which flows back to the scraper evaporator, base oil close to the bottom is circulated and flows back to the middle upper part of the rectifying tower for secondary evaporation, and unqualified oil products enter a second-stage evaporator for secondary evaporation treatment;
and g, adopting argil to refine the second-line base oil and the third-line base oil in the second-line receiving tank and the third-line receiving tank, adding argil into the first refined stripping tank and the second refined stripping tank which are provided with stirring devices to mix and decolor, directly introducing 0.3MPA saturated steam to strip, removing impurities in the base oil, then passing through a vertical automatic filter, obtaining the filtered base oil which is a finished product (the second-line base oil and the third-line base oil), and cooling and then entering a finished product tank.
The invention relates to a further improvement of a waste mineral oil recovery treatment process, which is characterized in that in the step a, a raw material storage oil tank also receives waste oil recovered from waste emulsion.
The invention further improves the process for recovering and treating the waste mineral oil, and the flocculating agent separated in the step c is added into a flocculation blending tank.
Compared with the prior art, the invention has the beneficial effects that:
the rectification process of the rectification tower realizes the recutting of the waste mineral oil fraction, has safe process steps, less environmental pollution and higher yield; on the other hand, gas-phase oil and liquid-phase oil can be repeatedly treated among the two-stage evaporator, the scraper evaporator and the rectifying tower, so that the effect of the treatment process is ensured.
Drawings
FIG. 1 is a schematic structural view of the present invention;
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
As shown in FIG. 1, a process for recovering and treating waste mineral oil comprises the following steps,
a, detecting solid content of waste mineral oil, dividing the waste mineral oil into low-solid-content waste mineral oil and high-solid-content waste mineral oil, putting the low-solid-content waste mineral oil into a filtering structure with a grating, filtering larger impurities, periodically cleaning the impurities, enabling the low-solid-content waste mineral oil to pass through the filtering structure and then enter a raw material storage oil tank, and enabling the raw material storage oil tank to be also connected with waste emulsion to recover the treated waste oil;
b, putting the high-solid-content waste mineral oil obtained in the step a into a flocculation blending tank, adding a flocculating agent, and stirring at normal temperature and normal pressure;
c, blending the waste mineral oil by a flocculation blending tank, then feeding the waste mineral oil into a three-phase separator, separating out a flocculating agent, oil residue and the waste mineral oil, feeding the waste mineral oil into an intermediate tank, and adding the separated flocculating agent into the flocculation blending tank again; step b, directly adding the low-solid-content waste mineral oil in the raw oil storage tank into a flocculation tank, adding no flocculant, separating out water after three-phase centrifugation, mixing the oil phase with other waste mineral oil in the raw oil storage tank, and performing circulation in step b, wherein the water phase is directly sent to an emulsion workshop for treatment;
d, adding a small amount of flocculant into the intermediate tank, continuously stirring, and performing a reduced pressure distillation process;
e, enabling the waste mineral oil in the intermediate tank to enter a first-stage evaporator, performing pressure reduction (-0.08Mpa) treatment on the first-stage pressure-reduction evaporator by adopting a liquid ring vacuum pump, controlling the first-stage evaporation temperature at 200-220 ℃, performing secondary condensation on the evaporated water-oil mixture, pumping the water-oil mixture into an oil-water standing separation tank through a pipeline, discharging the separated water into a waste emulsion treatment system, and burning the waste oil in an incinerator; the liquid phase evaporated enters a second-stage evaporator, liquid oil at the bottom of the second-stage evaporator is pumped into a scraper evaporator, the gas phase directly enters a rectifying tower, the liquid oil is gasified in the scraper evaporator, the gas phase is introduced into the rectifying tower from the top of the scraper evaporator by vacuum, residual oil is removed by a scraper, the residual oil enters a bottom oil residue receiving tank, and then the residual oil residue is pumped into an oil residue storage tank;
f, carrying out reduced pressure distillation in the rectifying tower, controlling the temperature at the top of the reduced pressure rectifying tower to be 170-200 ℃, and under the condition that the vacuum degree is about-0.098 MPa (40mmHg), taking the fraction at the top of the reduced pressure rectifying tower as a first-line base oil gas, condensing and recovering the first-line base oil gas, and then, receiving the first-line base oil gas by an overhead oil storage tank to obtain first-line base oil; controlling the temperature of the reduced pressure rectifying tower to be about 250-270 ℃, and flowing the required liquid oil into a second-line receiving tank under the condition that the vacuum degree is about 30mmHg, and flowing the high-temperature difference into a first refining stripping tank; controlling the temperature of the reduced pressure rectifying tower to be 290-310 ℃, and flowing the required liquid oil into a three-line receiving tank under the condition of a vacuum degree of about 30mmHg, and flowing the high-temperature difference into a second refining stripping tank; residual liquid of the remaining heavy components is tower bottom oil which flows back to the scraper evaporator, base oil close to the bottom is circulated and flows back to the middle upper part of the rectifying tower for secondary evaporation, and unqualified oil products enter a second-stage evaporator for secondary evaporation treatment;
and g, adopting argil to refine the second-line base oil and the third-line base oil in the second-line receiving tank and the third-line receiving tank, adding argil into the first refined stripping tank and the second refined stripping tank which are provided with stirring devices to mix and decolor, directly introducing 0.3MPA saturated steam to strip, removing impurities in the base oil, then passing through a vertical automatic filter, obtaining the filtered base oil which is a finished product (the second-line base oil and the third-line base oil), and cooling and then entering a finished product tank. The waste gas generated by the first and second refining stripping tanks is treated by vacuum condensation and recovery of non-condensable gas, the filtered clay residue is incinerated in a matched incineration system, and the generated water and oil are treated in an oil-water standing separation tank.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (3)
1. A waste mineral oil recovery treatment process is characterized in that: comprises the following steps of (a) carrying out,
a, detecting solid content of waste mineral oil, dividing the waste mineral oil into low-solid-content waste mineral oil and high-solid-content waste mineral oil, putting the low-solid-content waste mineral oil into a filtering structure with a grating, and enabling the low-solid-content waste mineral oil to enter a raw material storage oil tank after passing through the filtering structure;
b, putting the high-solid-content waste mineral oil in the step a into a flocculation blending tank;
c, blending the waste mineral oil through a flocculation blending tank, then feeding the waste mineral oil into a three-phase separator, separating out a flocculating agent, oil residues and the waste mineral oil, feeding the waste mineral oil into an intermediate tank, directly feeding the waste mineral oil with low solid content in a raw oil storage tank into a flocculation tank, not adding the flocculating agent, separating out the water through three-phase centrifugation, feeding the oil phase into a raw oil storage tank, mixing the oil phase with other waste mineral oil, then performing the circulation of the step b, and directly feeding the water phase into an emulsion workshop for treatment;
d, adding a small amount of flocculant into the intermediate tank, continuously stirring, and performing a reduced pressure distillation process;
e, enabling the waste mineral oil in the intermediate tank to enter a first-stage evaporator, pumping a distilled water-oil mixture into an oil-water separation tank through a pipeline after secondary condensation, enabling a liquid phase to enter a second-stage evaporator, pumping liquid oil at the bottom of the second-stage evaporator into a scraper evaporator, directly enabling a gas phase to enter a rectifying tower, gasifying the liquid oil in the scraper evaporator, introducing the gas phase into the rectifying tower from the top of the scraper evaporator by vacuum, removing residual oil by a scraper, enabling the residual oil to enter a bottom oil residue receiving tank, and pumping the residual oil into an oil residue storage tank;
f, carrying out reduced pressure distillation in the rectifying tower, controlling the temperature at the top of the reduced pressure rectifying tower to be 170-200 ℃, and under the condition that the vacuum degree is about-0.098 MPa (40mmHg), taking the fraction at the top of the reduced pressure rectifying tower as a first-line base oil gas, condensing and recovering the first-line base oil gas, and then, receiving the first-line base oil gas by an overhead oil storage tank to obtain first-line base oil; controlling the temperature of the reduced pressure rectifying tower to be about 250-270 ℃, and flowing the required liquid oil into a second-line receiving tank under the condition that the vacuum degree is about 30mmHg, and flowing the high-temperature difference into a first refining stripping tank; controlling the temperature of the reduced pressure rectifying tower to be 290-310 ℃, and flowing the required liquid oil into a three-line receiving tank under the condition of a vacuum degree of about 30mmHg, and flowing the high-temperature difference into a second refining stripping tank; residual liquid of the remaining heavy components is tower bottom oil which flows back to the scraper evaporator, base oil close to the bottom is circulated and flows back to the middle upper part of the rectifying tower for secondary evaporation, and unqualified oil products enter a second-stage evaporator for secondary evaporation treatment;
and g, adopting argil to refine the second-line base oil and the third-line base oil in the second-line receiving tank and the third-line receiving tank, adding argil into the first refined stripping tank and the second refined stripping tank which are provided with stirring devices to mix and decolor, directly introducing 0.3MPA saturated steam to strip, removing impurities in the base oil, then passing through a vertical automatic filter, obtaining the filtered base oil which is a finished product (the second-line base oil and the third-line base oil), and cooling and then entering a finished product tank.
2. The process of claim 1, wherein the waste mineral oil recovery treatment process comprises the following steps: in the step a, the raw material storage tank also receives waste oil reclaimed from the waste emulsion.
3. The process of claim 1, wherein the waste mineral oil recovery treatment process comprises the following steps: and c, adding the flocculant separated in the step c into a flocculation blending tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111140487.XA CN113698959A (en) | 2021-09-28 | 2021-09-28 | Waste mineral oil recovery treatment process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111140487.XA CN113698959A (en) | 2021-09-28 | 2021-09-28 | Waste mineral oil recovery treatment process |
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| CN113698959A true CN113698959A (en) | 2021-11-26 |
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| CN202111140487.XA Pending CN113698959A (en) | 2021-09-28 | 2021-09-28 | Waste mineral oil recovery treatment process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114989861A (en) * | 2022-05-18 | 2022-09-02 | 余金珠 | Recycling system of waste mineral oil |
| CN115305143A (en) * | 2022-09-14 | 2022-11-08 | 重庆中吉达环保科技有限公司 | Method for refining waste mineral oil |
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| CN106916604A (en) * | 2017-04-07 | 2017-07-04 | 重庆君利丰环保有限公司 | Using the method for blast furnace blowing mode harmlessness disposing waste mineral oil |
| CN108485790A (en) * | 2018-03-26 | 2018-09-04 | 福斯特惠勒（河北）工程设计有限公司 | A method of improving regenerating waste oil treating capacity |
| CN111004646A (en) * | 2019-12-30 | 2020-04-14 | 山东东顺环保科技有限公司 | Recovery process and recovery system for waste mineral oil |
| CN111394123A (en) * | 2020-04-21 | 2020-07-10 | 云南新昊环保科技有限公司 | Process for refining regenerated base oil of lubricating oil from waste mineral oil solvent |
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2021
- 2021-09-28 CN CN202111140487.XA patent/CN113698959A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106916604A (en) * | 2017-04-07 | 2017-07-04 | 重庆君利丰环保有限公司 | Using the method for blast furnace blowing mode harmlessness disposing waste mineral oil |
| CN108485790A (en) * | 2018-03-26 | 2018-09-04 | 福斯特惠勒（河北）工程设计有限公司 | A method of improving regenerating waste oil treating capacity |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114989861A (en) * | 2022-05-18 | 2022-09-02 | 余金珠 | Recycling system of waste mineral oil |
| CN114989861B (en) * | 2022-05-18 | 2024-02-09 | 梁山德润能源有限公司 | Recycling system of waste mineral oil |
| CN115305143A (en) * | 2022-09-14 | 2022-11-08 | 重庆中吉达环保科技有限公司 | Method for refining waste mineral oil |
| CN115305143B (en) * | 2022-09-14 | 2023-04-07 | 重庆中吉达环保科技有限公司 | Method for refining waste mineral oil |
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