CN109897723A - A kind of preprocess method of waste lubricant oil regeneration production - Google Patents
A kind of preprocess method of waste lubricant oil regeneration production Download PDFInfo
- Publication number
- CN109897723A CN109897723A CN201910223279.2A CN201910223279A CN109897723A CN 109897723 A CN109897723 A CN 109897723A CN 201910223279 A CN201910223279 A CN 201910223279A CN 109897723 A CN109897723 A CN 109897723A
- Authority
- CN
- China
- Prior art keywords
- lubricant oil
- preprocess method
- waste
- regeneration production
- waste lubricant
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of preprocess methods of waste lubricant oil regeneration production, are related to the preconditioning technique field of waste lubricant oil regeneration production, specially following processing step: (a) hot settlement treatment；(b) flash distillation process；(c) inorganic membrane filtration；(d) it is evaporated under reduced pressure；(e) plus hydrogen regenerates；(f) atmospheric and vacuum distillation.The preprocess method of waste lubricant oil regeneration production, using inoranic membrane pretreating process, utilize the unique structure of membrane material itself, and its there is high screening precision, the mechanical admixture in waste lubricating oil can effectively be removed, also there is preferable removal effect to metal and easy coking substance simultaneously, it can be avoided subsequent distillation equipment coking problem, simultaneously, the preprocess method, while meeting hydrogenation plant feed needs, greatly simplify the pretreatment process of non-lubricated oil, improve the stability of integrated artistic, and the mode of cross-flow filtration reduces film surface pollution layer, it ensure that higher purification efficiency and the longer cycle of operation.
Description
Technical field
The present invention relates to the preconditioning technique field of waste lubricant oil regeneration production, specially a kind of waste lubricant oil regeneration production
Preprocess method.
Background technique
As industry continues to develop, the usage amount of lubricating oil is increasing, and the yield of waste lubrication oil is caused also to be passed year by year
Increase, the wasting of resources caused by the unreasonable discarding of waste lubricating oil and problem of environmental pollution are also increasingly by the weight of national governments
Depending on relative to simply using waste lubricating oil as offal treatment mode, waste lubricant oil regeneration can take into account resource reclaim and ring
Both sides demand is protected in border, and the pollutant in waste lubricating oil mainly has moisture, greasy filth, colloid, asphalitine, additive and its divides
Solve the substances such as object, organic acid and its esters, hetero atom (S, N, O and Cl) compound and condensed aromatics.
Common waste lubricating oil treatment process is broadly divided into three classes both at home and abroad: the clay-filtered regeneration technology of sulfuric acid-, distillation-
Solvent refining processes and add hydrogen regeneration technology, wherein meeting during handling waste lubricating oil of the clay-filtered regeneration technology of sulfuric acid-
Generate a large amount of sour gas sulfur dioxide and intractable acid sludge, sour water, clay dregs, burn into contaminated equipment and environment, gradually by
It eliminates；Distillation-solvent refining processes are domestic with technique, there is the easy coking of waste lubricating oil in distillation heating process, furfural essence
System is big using furfural amount, and energy consumption is high, NMP is expensive, facile hydrolysis, corrodes equipment and is only capable of production I class base oil etc. and is many
Disadvantage, in addition, above two technique causes the rate of recovery lower only by the impurity in waste lubricating oil as offal treatment, and also
A large amount of harmful side product can be generated；Hydrogenation technique can convert partial impurities in waste lubricating oil such as colloid, asphalitine etc.
For lube base oil component or light hydrocarbons, improve the regeneration yield and by-product value of waste lubricating oil, thus gradually at
For the mainstream technology of waste lubricant oil regeneration.
Pretreating process more mature at present is propane extracting and is evaporated under reduced pressure, and cooperates flash distillation or gas stripping process, though
It is so able to produce out the pretreatment oil for meeting hydrogenation requirements, but the device is complicated, distillation equipment coking problem is serious, and operating cost is high
And the rate of recovery is lower, is to lead to that waste lubricating oil integrally regenerates the not high key point of yield and waste generates most rings
Section, therefore, the improvement and innovation of pretreating process are to determine the main driving of waste lubricant oil by hydrogenation regeneration industry development speed.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of preprocess methods of waste lubricant oil regeneration production, solve
The problems mentioned above in the background art.
In order to achieve the above object, the present invention is achieved by the following technical programs: a kind of production of waste lubricant oil regeneration
Preprocess method, the preprocess method comprise the following steps that:
(a) hot settlement treatment: waste lubricating oil raw material is subjected to heat sink drop in raw material storage tank, removes partial impurities；
(b) flash distillation process: flashing after supernatant liquor heats up after the hot settlement treatment of step (a), removes light component
And water；
(c) inorganic membrane filtration: entering inorganic film device from inoranic membrane device portal for the waste lubricating oil after flash distillation, and inorganic
Enter membrane module after the interior circulation fluid mixing of film device to filter, removes metal and part easily coking substance；
(d) be evaporated under reduced pressure: liquid enters vacuum distillation apparatus after filter, carries out the cutting of weight component；
(e) plus hydrogen regenerates: target waste oil component addition hydrogenation plant being carried out plus hydrogen regenerates, wherein used plus hydrogen
Device includes three reactors for passing sequentially through piping connection, and protective agent and metal remover are wherein loaded in first reactor, the
Two reactors are built-in to be dosed hydrogen catalyst and is laid with antichlor on a catalyst, and aromatic hydrocarbon refining agent is loaded in third reactor；
(f) atmospheric and vacuum distillation: add oil product after hydrogen to enter atmospheric and vacuum distillation progress product segmentation, obtain different product.
Optionally, the hot settling temperature of raw material storage tank is 60~80 DEG C in the step (a), the sedimentation time ≮ 5h.
Optionally, the step (b) enters flash tank after clear liquid is warming up to 90~150 DEG C at the middle and upper levels, and flash vacuum degree is-
10~-80kPa.
Optionally, the inorganic film device in the step (c), filtering front and back pressure drop is 0.1~0.5MPa, and filtration temperature is
120~150 DEG C.
Optionally, the flow-rate ratio of the outer discharge capacity of the inorganic film device in the step (c), total feed and concentrate be (5~
10):1。
Optionally, the inorganic film device cleaning frequency in the step (c) is 10~15 days, utilizes in-site chemical cleaning system
System implements online restore using strainability of the chemical to inoranic membrane.
Optionally, the chemical is the dedicated chemical of SRMK-C02 type inoranic membrane.
Optionally, the vacuum distillation apparatus in the step (d), Top of Vacuum Tower absolute pressure are 20-60mmHg, temperature 40-
140 DEG C, wherein the overheated steam that vacuum distillation tower using temperature is 200-460 DEG C, pressure is 0.1-2.5MPa carries out vapour
It mentions, sloughs the impurity such as heavy constituent and carbon residue, obtain and add hydrogen distillate.
Optionally, the depth of cut of the vacuum distillation tower is 530 DEG C, wherein boiling range < 530 DEG C component is used as plus hydrogen evaporates
Oil is divided to enter follow-up hydrogenation device, the residual base oil of process >=530 DEG C is as asphalt stock or fuel oil processing.
The present invention provides a kind of preprocess methods of waste lubricant oil regeneration production, have following the utility model has the advantages that the useless profit
The preprocess method of lubricating oil regeneration production utilizes the unique structure of membrane material itself and its institute using inoranic membrane pretreating process
With high screening precision, the mechanical admixture in waste lubricating oil can be effectively removed, while also being had to metal and easy coking substance
Preferable removal effect can be avoided subsequent distillation equipment coking problem；The preprocess method is wanted meeting hydrogenation plant charging
While asking, greatly simplify the pretreatment process of non-lubricated oil, improves the stability of integrated artistic, and cross-flow filtration
Mode reduces film surface pollution layer, ensure that higher purification efficiency and the longer cycle of operation, realizes waste lubricant oil by hydrogenation mistake
The stabilization of journey, guarantees the quality of hydrogenated products, while cooperating reduced pressure distillation technique, the oil product of isolated different viscosities；This is whole
Body pretreating process is higher for the rate of recovery, the separative efficiency of waste lubricating oil, energy conservation and environmental protection and be easy to engineering amplification.
Specific embodiment
The technical scheme in the embodiments of the invention will be clearly and completely described below, it is clear that described implementation
Example is only a part of the embodiment of the present invention, and instead of all the embodiments, based on the embodiments of the present invention, this field is common
Technical staff's every other embodiment obtained without making creative work belongs to the model that the present invention protects
It encloses.
Embodiment 1
A kind of preprocess method of waste lubricant oil regeneration production, comprises the following steps that:
(a) waste lubricating oil raw material hot settlement treatment: is subjected to heat sink drop, the hot settling temperature of raw material storage tank in raw material storage tank
It is 80 DEG C, sedimentation time 8h；The waste lubricating oil that raw material storage tank is newly added in heat sink drop treatment process can be in the process of cold and hot convection current
In be sufficiently mixed with material original in tank realization, while bulky grain mechanical admixture is settled down to tank bottom, realizes impurity and raw material
Initial gross separation achievees the purpose that remove partial impurities；
(b) supernatant liquor flash distillation process: is warming up to 105 DEG C of entrance by heat exchanger after the hot settlement treatment of step (a)
Flash tank is flashed, and light component and water are removed, and flash vacuum degree is -50kPa；
(c) inorganic membrane filtration: entering inorganic film device from inoranic membrane device portal for the waste lubricating oil after flash distillation, and inorganic
Enter membrane module after the interior circulation fluid mixing of film device to filter, filtering front and back pressure drop is 0.15MPa, and filtration temperature is 150 DEG C, is taken off
Except metal and part easily coking substance；To guarantee material balance in system object, while liquid after generating filter, it is also necessary to be discharged one
The flow-rate ratio of the outer discharge capacity of partial concentration liquid, total feed and concentrate is 10:1；
(d) be evaporated under reduced pressure: liquid enters vacuum distillation apparatus after filter, and the Top of Vacuum Tower absolute pressure of vacuum distillation apparatus is
40mmHg, temperature are 120 DEG C；
Vacuum distillation tower using temperature is 360 DEG C, the overheated steam that pressure is 2.0MPa is stripped, and depth of cut is
530℃；Boiling range<530 DEG C component is as adding hydrogen distillate to enter follow-up hydrogenation device, and the residual base oil of process>=530 DEG C is as drip
Green raw material or fuel oil processing；
(e) plus hydrogen regenerates: target waste oil component being entered hydrogenation plant and carries out adding hydrogen regeneration, used hydrogenation plant packet
Three reactors for passing sequentially through piping connection are included, protective agent and metal remover, the second reaction are wherein loaded in first reactor
Device is built-in to be dosed hydrogen catalyst and is laid with antichlor on a catalyst, and aromatic hydrocarbon refining agent is loaded in third reactor；Wherein made
Various catalyst can select commercial catalyst by property, can also be determined by those skilled in the art according to actual needs
Select conventional use of catalyst；
(f) atmospheric and vacuum distillation: the product after adding hydrogen is after air lift removes sour gas, into atmospheric and vacuum distillation unit, according to boiling range
Fraction cutting is carried out with viscosity, three side lines are set, 3 kinds of products are obtained.
Wherein, the inorganic film device cleaning frequency described in step (c) is 15 days, using in-site chemical cleaning system, is used
SRMK-C02 type chemical implements online recovery to the strainability of inoranic membrane, is not necessarily to membrane tube recoil and membrane tube disassembly again
It is raw, the blocking to fenestra such as heavy metal, ash content and microparticle such as carbon black, particle can be effectively removed, after chemical cleaning
Inoranic membrane can restore higher flux, it is ensured that the long-term operation of system.
In embodiment 1, feedstock property is as shown in table 1 below:
| Analysis project | Raw material |
| 80 DEG C of viscosity (mm2/s) | 17.5 |
| Acid value (mgKOH/g) | 0.88 |
| S content % (w) | 0.36 |
| N content (mg/kg) | 1080 |
| Carbon residue % | 1.19 |
| Ash content % | 0.568 |
| It is saturated part, % | 97.88 |
| Fragrant part, % | 0.19 |
| Colloid, % | 1.54 |
| Asphalitine, % | 0.39 |
| IBP/10% | 165/372.8 |
| 30%/50% | 421.6/452.6 |
| 70%/90% | 492.4/578.2 |
| 95%/FBP | 749.8 (95.4%) |
| Total metal (ppm) | 2721.83 |
Table 1
Contrast on effect is as shown in table 2 below after inoranic membrane purification:
| Analysis project | Raw material | Penetrating fluid | Removal efficiency |
| 80 DEG C of viscosity (mm2/s) | 17.5 | 9.236 | |
| Acid value (mgKOH/g) | 0.88 | 0.72 | |
| S content % (w) | 0.36 | 0.28 | 22.2% |
| N content (mg/kg) | 1080 | 570 | 47.2% |
| Carbon residue % | 1.19 | 0.15 | 87.4% |
| Ash content % | 0.568 | 0.063 | 88.9% |
| It is saturated part, % | 97.88 | 98.69 | |
| Fragrant part, % | 0.19 | 0.12 | |
| Colloid, % | 1.54 | 1.16 | |
| Asphalitine, % | 0.39 | 0.03 | |
| IBP/10% | 165/372.8 | 178.4/374.2 | |
| 30%/50% | 421.6/452.6 | 420.2/449 | |
| 70%/90% | 492.4/578.2 | 486/552.2 | |
| 95%/FBP | 749.8 (95.4%) | 750 (97.1%) | |
| Total metal (ppm) | 2721.83 | 146.11 | 94.6% |
Table 2
Add product property after hydrogen as shown in table 3 below:
Table 3
Embodiment 2
A kind of preprocess method of waste lubricant oil regeneration production, the preprocess method comprise the following steps that:
(a) hot settlement treatment: waste lubricating oil raw material is subjected to heat sink drop in raw material storage tank, removes partial impurities, wherein
The hot settling temperature of raw material storage tank is 70 DEG C, sedimentation time 6.5-7h；
(b) flash distillation process: flashing after supernatant liquor heats up after the hot settlement treatment of step (a), removes light component
And water, wherein supernatant liquor enters flash tank after heat exchanger is warming up to 100 DEG C, and flash vacuum degree is -30kPa；
(c) inorganic membrane filtration: entering inorganic film device from inoranic membrane device portal for the waste lubricating oil after flash distillation, and inorganic
Enter membrane module after the interior circulation fluid mixing of film device to filter, removes metal and part easily coking substance, wherein inorganic film device
Filtering before and after pressure drop be 0.13MPa, filtration temperature is 135 DEG C, and the flow-rate ratio of the outer discharge capacity of total feed and concentrate is 8:1；
Further, the inorganic film device cleaning frequency is 13 days, using in-site chemical cleaning system, using chemical
Online restore is implemented to the strainability of inoranic membrane, wherein chemical is the dedicated chemical cleaning of SRMK-C02 type inoranic membrane
Agent；
(d) be evaporated under reduced pressure: liquid enters vacuum distillation apparatus after filter, carries out the cutting of weight component, wherein vacuum distillation apparatus
In, Top of Vacuum Tower absolute pressure is 30mmHg, and temperature is 100 DEG C, wherein vacuum distillation tower using temperature is 280 DEG C, pressure is
The overheated steam of 1.6MPa is stripped, and the impurity such as heavy constituent and carbon residue are sloughed, and is obtained and is added hydrogen distillate；
Further, the depth of cut of vacuum distillation tower is 530 DEG C, wherein boiling range < 530 DEG C component is used as plus hydrogen fraction
Oil enters follow-up hydrogenation device, and the residual base oil of process >=530 DEG C is as asphalt stock or fuel oil processing；
(e) plus hydrogen regenerates: target waste oil component addition hydrogenation plant being carried out plus hydrogen regenerates, wherein used plus hydrogen
Device includes three reactors for passing sequentially through piping connection, and protective agent and metal remover are wherein loaded in first reactor, the
Two reactors are built-in to be dosed hydrogen catalyst and is laid with antichlor on a catalyst, and aromatic hydrocarbon refining agent is loaded in third reactor；
(f) atmospheric and vacuum distillation: add oil product after hydrogen to enter atmospheric and vacuum distillation progress product segmentation, obtain different product.
Embodiment 3
A kind of preprocess method of waste lubricant oil regeneration production, the preprocess method comprise the following steps that:
(a) hot settlement treatment: waste lubricating oil raw material is subjected to heat sink drop in raw material storage tank, removes partial impurities, wherein
The hot settling temperature of raw material storage tank is 60 DEG C, sedimentation time 6h；
(b) flash distillation process: flashing after supernatant liquor heats up after the hot settlement treatment of step (a), removes light component
And water, wherein supernatant liquor enters flash tank after heat exchanger is warming up to 95 DEG C, and flash vacuum degree is -15kPa；
(c) inorganic membrane filtration: entering inorganic film device from inoranic membrane device portal for the waste lubricating oil after flash distillation, and inorganic
Enter membrane module after the interior circulation fluid mixing of film device to filter, removes metal and part easily coking substance, wherein inorganic film device
Filtering before and after pressure drop be 0.1MPa, filtration temperature is 125 DEG C, and the flow-rate ratio of the outer discharge capacity of total feed and concentrate is 6:1；
Further, the inorganic film device cleaning frequency is 10 days, using in-site chemical cleaning system, using chemical
Online restore is implemented to the strainability of inoranic membrane, wherein chemical is the dedicated chemical cleaning of SRMK-C02 type inoranic membrane
Agent；
(d) be evaporated under reduced pressure: liquid enters vacuum distillation apparatus after filter, carries out the cutting of weight component, wherein vacuum distillation apparatus
In, Top of Vacuum Tower absolute pressure is 20mmHg, and temperature is 65 DEG C, wherein vacuum distillation tower using temperature is 220 DEG C, pressure is
The overheated steam of 0.8MPa is stripped, and the impurity such as heavy constituent and carbon residue are sloughed, and is obtained and is added hydrogen distillate；
Further, the depth of cut of vacuum distillation tower is 530 DEG C, wherein boiling range < 530 DEG C component is used as plus hydrogen fraction
Oil enters follow-up hydrogenation device, and the residual base oil of process >=530 DEG C is as asphalt stock or fuel oil processing；
(e) plus hydrogen regenerates: target waste oil component addition hydrogenation plant being carried out plus hydrogen regenerates, wherein used plus hydrogen
Device includes three reactors for passing sequentially through piping connection, and protective agent and metal remover are wherein loaded in first reactor, the
Two reactors are built-in to be dosed hydrogen catalyst and is laid with antichlor on a catalyst, and aromatic hydrocarbon refining agent is loaded in third reactor；
(f) atmospheric and vacuum distillation: add oil product after hydrogen to enter atmospheric and vacuum distillation progress product segmentation, obtain different product.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Anyone skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (9)
1. a kind of preprocess method of waste lubricant oil regeneration production, it is characterised in that: the preprocess method includes following technique step
It is rapid:
(a) hot settlement treatment: waste lubricating oil raw material is subjected to heat sink drop in raw material storage tank, removes partial impurities；
(b) flash distillation process: flashing after supernatant liquor heats up after the hot settlement treatment of step (a), removes light component and water；
(c) inorganic membrane filtration: the waste lubricating oil after flash distillation is entered into inorganic film device from inoranic membrane device portal, is filled with inoranic membrane
Enter membrane module after the interior circulation fluid mixing set to filter, removes metal and part easily coking substance；
(d) be evaporated under reduced pressure: liquid enters vacuum distillation apparatus after filter, carries out the cutting of weight component；
(e) plus hydrogen regenerates: target waste oil component addition hydrogenation plant being carried out plus hydrogen regenerates, wherein used hydrogenation plant
Three reactors including passing sequentially through piping connection wherein load protective agent and metal remover in first reactor, second is anti-
It answers device is built-in to dose hydrogen catalyst and be laid with antichlor on a catalyst, aromatic hydrocarbon refining agent is loaded in third reactor；
(f) atmospheric and vacuum distillation: add oil product after hydrogen to enter atmospheric and vacuum distillation progress product segmentation, obtain different product.
2. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(a) the hot settling temperature of raw material storage tank is 60~80 DEG C in, the sedimentation time ≮ 5h.
3. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(b) enter flash tank after clear liquid is warming up to 90~150 DEG C at the middle and upper levels, flash vacuum degree is -10~-80kPa.
4. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(c) the inorganic film device in, filtering front and back pressure drop are 0.1~0.5MPa, and filtration temperature is 120~150 DEG C.
5. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(c) flow-rate ratio of the outer discharge capacity of the inorganic film device in, total feed and concentrate is (5~10): 1.
6. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(c) the inorganic film device cleaning frequency in is 10~15 days, using in-site chemical cleaning system, using chemical to inorganic
The strainability of film implements online restore.
7. a kind of preprocess method of waste lubricant oil regeneration production according to claim 6, it is characterised in that: the chemistry
Cleaning agent is the dedicated chemical of SRMK-C02 type inoranic membrane.
8. a kind of preprocess method of waste lubricant oil regeneration production according to claim 1, it is characterised in that: the step
(d) vacuum distillation apparatus in, Top of Vacuum Tower absolute pressure are 20-60mmHg, and temperature is 40-140 DEG C, wherein vacuum distillation tower makes
It is stripped with the overheated steam that temperature is 200-460 DEG C, pressure is 0.1-2.5MPa, it is miscellaneous to slough heavy constituent and carbon residue etc.
Matter obtains and adds hydrogen distillate.
9. a kind of preprocess method of waste lubricant oil regeneration production according to claim 8, it is characterised in that: the decompression
The depth of cut of destilling tower is 530 DEG C, wherein boiling range < 530 DEG C component is flowed as adding hydrogen distillate to enter follow-up hydrogenation device
The residual base oil of journey >=530 DEG C is as asphalt stock or fuel oil processing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910223279.2A CN109897723A (en) | 2019-03-22 | 2019-03-22 | A kind of preprocess method of waste lubricant oil regeneration production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910223279.2A CN109897723A (en) | 2019-03-22 | 2019-03-22 | A kind of preprocess method of waste lubricant oil regeneration production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109897723A true CN109897723A (en) | 2019-06-18 |
Family
ID=66953831
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910223279.2A Pending CN109897723A (en) | 2019-03-22 | 2019-03-22 | A kind of preprocess method of waste lubricant oil regeneration production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109897723A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111575101A (en) * | 2020-04-09 | 2020-08-25 | 南京弘顺和生物科技有限公司 | Waste lubricating oil regeneration device and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5772900A (en) * | 1994-06-22 | 1998-06-30 | Noritake Co., Limited | Method and apparatus for reclaiming used working fluid |
| CN103432816A (en) * | 2013-07-29 | 2013-12-11 | 南京工业大学 | Method and device for recovering waste cleaning solvent |
| CN105907452A (en) * | 2016-04-29 | 2016-08-31 | 中国石油大学(华东) | Combined technological method for recycling waste lubricating oil by means of heat treatment |
| CN108085060A (en) * | 2018-01-22 | 2018-05-29 | 常州菲纳斯能源科技有限公司 | Waste lubricant oil by hydrogenation process for purification and hydrofinishing system |
| CN207913535U (en) * | 2017-08-24 | 2018-09-28 | 江苏赛瑞迈科新材料有限公司 | Hollow fiber ceramic membrane and its application apparatus |
-
2019
- 2019-03-22 CN CN201910223279.2A patent/CN109897723A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5772900A (en) * | 1994-06-22 | 1998-06-30 | Noritake Co., Limited | Method and apparatus for reclaiming used working fluid |
| CN103432816A (en) * | 2013-07-29 | 2013-12-11 | 南京工业大学 | Method and device for recovering waste cleaning solvent |
| CN105907452A (en) * | 2016-04-29 | 2016-08-31 | 中国石油大学(华东) | Combined technological method for recycling waste lubricating oil by means of heat treatment |
| CN207913535U (en) * | 2017-08-24 | 2018-09-28 | 江苏赛瑞迈科新材料有限公司 | Hollow fiber ceramic membrane and its application apparatus |
| CN108085060A (en) * | 2018-01-22 | 2018-05-29 | 常州菲纳斯能源科技有限公司 | Waste lubricant oil by hydrogenation process for purification and hydrofinishing system |
Non-Patent Citations (1)
| Title |
|---|
| 赵麦玲，邓义林: "废润滑油再生工艺技术", 《化工设计通讯》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111575101A (en) * | 2020-04-09 | 2020-08-25 | 南京弘顺和生物科技有限公司 | Waste lubricating oil regeneration device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103880242B (en) | A kind of coal chemical industrial waste water advanced treatment process | |
| CN103482715B (en) | A kind of high concentrated organic wastewater evaporation concentration treatment process | |
| CN109250854A (en) | The processing method of semi-coke wastewater | |
| CN107312568B (en) | Waste mineral oil catalytic cracking comprehensive utilization system and processing technology thereof | |
| CN106145426A (en) | In a kind of coal chemical industrial waste water, carbolic oil is combined removing system and processes technique | |
| CN1986390A (en) | Process of purifying and recovering waste sulfuric acid containing organic impurity | |
| CN105694962A (en) | Regeneration technology for waste mineral oil | |
| CN109161433A (en) | A kind of process of waste mineral oil regenerated resourcesization disposition | |
| Song et al. | Low-temperature hydrothermal carbonization of fresh pig manure: effects of temperature on characteristics of hydrochars | |
| CN105036443A (en) | Method and device for treating phenol ammonia wastewater in single-tower stripping mode by recovering steam condensate heat | |
| CN102153449A (en) | Continuous refining separation device and method for coal gasification crude phenol | |
| CN107445802A (en) | A kind of method that ethylene glycol and acetaldehyde are reclaimed in polyester waste water | |
| CN108821308B (en) | Method and device for preparing high-concentration ammonia water by using coking residual ammonia water | |
| CN108264946A (en) | A kind of harmlessness disposing of waste mineral oil utilizes method | |
| CN105923610A (en) | Novel process of acetylene purification and waste acid regeneration | |
| CN110330988A (en) | A kind of wholegrain diameter coal cracking sub-prime utilizes production technology | |
| CN109897723A (en) | A kind of preprocess method of waste lubricant oil regeneration production | |
| CN102634381B (en) | System and method for treating benzene-contained separating water of coking benzol | |
| CN208250114U (en) | A kind of coal chemical industry technique waste water advanced treatment device | |
| CN203781978U (en) | Advanced treatment equipment for coal chemical industrial wastewater | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN104150673A (en) | System and method for treating and recycling methanol aromatization wastewater | |
| CN102452756A (en) | Treatment method of wastewater from acrylonitrile production device by propylene ammoxidation | |
| CN103849453B (en) | Waste emulsified oil purifying method | |
| CN103212424B (en) | Method for recycling glycol and acetaldehyde in polyester waste water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190618 |
|
| RJ01 | Rejection of invention patent application after publication |