CN107982950A - A kind of useless transformer oil recovery method - Google Patents
A kind of useless transformer oil recovery method Download PDFInfo
- Publication number
- CN107982950A CN107982950A CN201711137582.8A CN201711137582A CN107982950A CN 107982950 A CN107982950 A CN 107982950A CN 201711137582 A CN201711137582 A CN 201711137582A CN 107982950 A CN107982950 A CN 107982950A
- Authority
- CN
- China
- Prior art keywords
- level
- heavy constituent
- transformer oil
- light component
- distillation
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/12—Molecular distillation
Abstract
The invention discloses a kind of useless transformer oil recovery method, it uses three-level or secondary molecules to distill and recycled, and wherein afterbody molecular distillation pressure is 0.1~200Pa, and molecular distillation temperature is 60~200 DEG C, and obtained light component is transformer oil.The present invention removes useless transformer oil impurities, recover the purity of transformer oil, transformer oil is set to reuse, whole removal process is pure physical process, and without using any chemical reagents and adsorbent, reclaimer operation expense is low, the rate of recovery is high, the material of pollution environment will not be produced, without considering the post processing problem of material therefor, realizes environmentally protective recovery method.
Description
Technical field
The present invention relates to scrap concrete process field, particularly a kind of useless transformer oil recovery method.
Background technology
Transformer oil includes mineral type transformer oil and plant type transformer oil.Existing transformer oil recovery method uses
Chemical reagent and adsorbent, such as Chinese patent：A kind of sorbent regeneration process (publication number of the plant transformer oil of deterioration
106867679A), used adsorbent includes hydrochloric acid solution, metabisulfite solution, sodium silicate solution, ammonium hydroxide, amino functional
Silica based materials and football alkene etc., processing method are complicated.
There are problem to have for existing recovery method：Chemical reagent and adsorbent can remain in oil recovery；Chemical reagent and suction
Secondary pollution of attached dose of the impurity to oil recovery；Absorption, filtering make oil loss big, and the rate of recovery reduces；Chemical reagent and absorption
The post processing of agent causes serious pollution to the environment, it is costly to post-process.
The content of the invention
To solve the above-mentioned problems, the object of the present invention is to provide a kind of useless transformer oil recovery method, without using any
Chemical reagent and adsorbent, reclaimer operation expense is low, and the rate of recovery is high, will not produce the material of pollution environment.
The object of the present invention is achieved like this：A kind of useless transformer oil recovery method, it is characterised in that：Using three-level or
Secondary molecules distillation is recycled, and wherein afterbody molecular distillation pressure be 0.1~200Pa, and molecular distillation temperature is 60~
200 DEG C, obtained light component is transformer oil.
The three-level molecular distillation technique is：First order molecular distillation pressure is 1000~10000Pa, and first order molecular distills
Temperature is 30~80 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, secondary molecules
Distillation pressure is 100~2000Pa, and secondary molecules vapo(u)rizing temperature is 40~120 DEG C, obtains two level light component and two level heavy constituent；
Two level heavy constituent carries out three-level molecular distillation, and three-level molecular distillation pressure is 0.1~200Pa, and three-level molecular distillation temperature is 60
~200 DEG C, obtain three-level light component and three-level heavy constituent.
Preferably, the three-level molecular distillation technique is：First order molecular distillation pressure is 2000~8000Pa, a fraction
Sub- vapo(u)rizing temperature is 40~70 DEG C, obtains level-one light component and level-one heavy constituent；The progress secondary molecules distillation of level-one heavy constituent, two
Level molecule distillation pressure is 300~2000Pa, and secondary molecules vapo(u)rizing temperature is 60~120 DEG C, obtains two level light component and two level
Heavy constituent；Two level heavy constituent carries out three-level molecular distillation, and three-level molecular distillation pressure is 1~200Pa, three-level molecular distillation temperature
For 60~200 DEG C, three-level light component and three-level heavy constituent are obtained.
The two-stage molecular distillation technique is：First order molecular distillation pressure is 1000~10000Pa, and first order molecular distills
Temperature is 40~120 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, two fractions
Sub- distillation pressure is 0.1~200Pa, and secondary molecules vapo(u)rizing temperature is 60~200 DEG C, obtains two level light component and is recombinated with two level
Point.
Preferably, the two-stage molecular distillation technique is：First order molecular distillation pressure is 2000~8000Pa, a fraction
Sub- vapo(u)rizing temperature is 50~120 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation,
Secondary molecules distillation pressure is 1~200Pa, and secondary molecules vapo(u)rizing temperature is 60~200 DEG C, obtains two level light component and two level weight
Component.
The transformer oil is mineral oil origin transformer oil.
The present invention removes useless transformer oil impurities, recovers the purity of transformer oil, transformer oil is repeated
Use, whole removal process is pure physical process, and without using any chemical reagents and adsorbent, reclaimer operation expense is low, recycling
Rate is high, will not produce the material of pollution environment, without considering the post processing problem of material therefor, realize environmentally protective recycling side
Method.
Embodiment
The present invention is a kind of useless transformer oil recovery method, is recycled using three-level or secondary molecules distillation, wherein most
Rear stage molecular distillation pressure is 0.1~200Pa, and molecular distillation temperature is 60~200 DEG C, and obtained light component is transformer
Oil.It is particularly suitable for mineral oil origin transformer oil.
The three-level molecular distillation technique is：First order molecular distillation pressure is 1000~10000Pa, and first order molecular distills
Temperature is 30~80 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, secondary molecules
Distillation pressure is 100~2000Pa, and secondary molecules vapo(u)rizing temperature is 40~120 DEG C, obtains two level light component and two level heavy constituent；
Two level heavy constituent carries out three-level molecular distillation, and three-level molecular distillation pressure is 0.1~200Pa, and three-level molecular distillation temperature is 60
~200 DEG C, obtain three-level light component and three-level heavy constituent.Preferably, the three-level molecular distillation technique is：First order molecular steams
It is 2000~8000Pa to evaporate pressure, and first order molecular vapo(u)rizing temperature is 40~70 DEG C, obtains level-one light component and level-one heavy constituent；One
Level heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure be 300~2000Pa, and secondary molecules vapo(u)rizing temperature is 60~
120 DEG C, obtain two level light component and two level heavy constituent；Two level heavy constituent carries out three-level molecular distillation, three-level molecular distillation pressure
For 1~200Pa, three-level molecular distillation temperature is 60~200 DEG C, obtains three-level light component and three-level heavy constituent.
The two-stage molecular distillation technique is：First order molecular distillation pressure is 1000~10000Pa, and first order molecular distills
Temperature is 40~120 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, two fractions
Sub- distillation pressure is 0.1~200Pa, and secondary molecules vapo(u)rizing temperature is 60~200 DEG C, obtains two level light component and is recombinated with two level
Point.Preferably, the two-stage molecular distillation technique is：First order molecular distillation pressure is 2000~8000Pa, and first order molecular steams
Temperature is evaporated for 50~120 DEG C, obtains level-one light component and level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, two level
Molecular distillation pressure is 1~200Pa, and secondary molecules vapo(u)rizing temperature is 60~200 DEG C, obtains two level light component and is recombinated with two level
Point.
Below by way of specific example, the invention will be further described.
Embodiment 1
Molecular distillation process is carried out, first order molecular distillation pressure is 2000Pa, and first order molecular vapo(u)rizing temperature is 40 DEG C, is obtained
Level-one light component and level-one heavy constituent.
Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 300Pa, and secondary molecules vapo(u)rizing temperature is
60 DEG C, obtain two level light component and two level heavy constituent.
Two level heavy constituent carries out three-level molecular distillation, and three-level molecular distillation pressure is 7Pa, and three-level molecular distillation temperature is 90
DEG C, obtain three-level light component and three-level heavy constituent.Three-level light component is transformer oil.
Embodiment 2
Molecular distillation process is carried out, first order molecular distillation pressure is 5000Pa, and first order molecular vapo(u)rizing temperature is 60 DEG C, is obtained
Level-one light component and level-one heavy constituent.
Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 100Pa, and secondary molecules vapo(u)rizing temperature is
150 DEG C, obtain two level light component and two level heavy constituent.Two level light component is transformer oil.
Embodiment 3
Molecular distillation process is carried out, first order molecular distillation pressure is 3000Pa, and first order molecular vapo(u)rizing temperature is 50 DEG C, is obtained
Level-one light component and level-one heavy constituent.
Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 400Pa, and secondary molecules vapo(u)rizing temperature is
70 DEG C, obtain two level light component and two level heavy constituent.
Two level heavy constituent carries out three-level molecular distillation, and three-level molecular distillation pressure is 40Pa, and three-level molecular distillation temperature is
110 DEG C, obtain three-level light component and three-level heavy constituent.Three-level light component is transformer oil.
Embodiment 4
Molecular distillation process is carried out, first order molecular distillation pressure is 8000Pa, and first order molecular vapo(u)rizing temperature is 70 DEG C, is obtained
Level-one light component and level-one heavy constituent.
Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 160Pa, and secondary molecules vapo(u)rizing temperature is
180 DEG C, obtain two level light component and two level heavy constituent.Two level light component is transformer oil.
Table 1 is the rate of recovery of embodiment 1-4 and the quality index of gained transformer oil, it can be seen that at the present invention
After reason, the transformer oil rate of recovery is high, and purity is recovered, and meets requirement, therefore can reuse.
Table 1.
Claims (6)
- A kind of 1. useless transformer oil recovery method, it is characterised in that：Recycled using three-level or secondary molecules distillation, wherein most Rear stage molecular distillation pressure is 0.1~200Pa, and molecular distillation temperature is 60~200 DEG C, and obtained light component is transformer Oil.
- 2. useless transformer oil recovery method according to claim 1, it is characterised in that：The three-level molecular distillation technique For：First order molecular distillation pressure is 1000~10000Pa, and first order molecular vapo(u)rizing temperature is 30~80 DEG C, obtains level-one light component With level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 100~2000Pa, two fractions Sub- vapo(u)rizing temperature is 40~120 DEG C, obtains two level light component and two level heavy constituent；Two level heavy constituent carries out three-level molecular distillation, Three-level molecular distillation pressure is 0.1~200Pa, and three-level molecular distillation temperature is 60~200 DEG C, obtains three-level light component and three-level Heavy constituent.
- 3. useless transformer oil recovery method according to claim 2, it is characterised in that：The three-level molecular distillation technique For：First order molecular distillation pressure is 2000~8000Pa, and first order molecular vapo(u)rizing temperature is 40~70 DEG C, obtain level-one light component with Level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 300~2000Pa, secondary molecules Vapo(u)rizing temperature is 60~120 DEG C, obtains two level light component and two level heavy constituent；The progress three-level molecular distillation of two level heavy constituent, three Level molecule distillation pressure is 1~200Pa, and three-level molecular distillation temperature is 60~200 DEG C, obtains three-level light component and is recombinated with three-level Point.
- 4. useless transformer oil recovery method according to claim 1, it is characterised in that：The two-stage molecular distillation technique For：First order molecular distillation pressure is 1000~10000Pa, and first order molecular vapo(u)rizing temperature is 40~120 DEG C, obtains level-one light component With level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 0.1~200Pa, secondary molecules Vapo(u)rizing temperature is 60~200 DEG C, obtains two level light component and two level heavy constituent.
- 5. useless transformer oil recovery method according to claim 4, it is characterised in that：The two-stage molecular distillation technique For：First order molecular distillation pressure is 2000~8000Pa, and first order molecular vapo(u)rizing temperature is 50~120 DEG C, obtains level-one light component With level-one heavy constituent；Level-one heavy constituent carries out secondary molecules distillation, and secondary molecules distillation pressure is 1~200Pa, and secondary molecules steam Temperature is evaporated for 60~200 DEG C, obtains two level light component and two level heavy constituent.
- 6. the useless transformer oil recovery method according to claim 1-5 any claims, it is characterised in that：Described Transformer oil is mineral oil origin transformer oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711137582.8A CN107982950B (en) | 2017-11-16 | 2017-11-16 | Method for recovering waste transformer oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711137582.8A CN107982950B (en) | 2017-11-16 | 2017-11-16 | Method for recovering waste transformer oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107982950A true CN107982950A (en) | 2018-05-04 |
| CN107982950B CN107982950B (en) | 2020-06-30 |
Family
ID=62031611
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711137582.8A Active CN107982950B (en) | 2017-11-16 | 2017-11-16 | Method for recovering waste transformer oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107982950B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4568428A (en) * | 1983-07-05 | 1986-02-04 | General Signal Corporation | Method and apparatus for vacuum distillation |
| RU2002796C1 (en) * | 1992-01-22 | 1993-11-15 | Насир Мамед оглы Алиев | Method of transformer oil preparation |
| CN101177646A (en) * | 2007-10-26 | 2008-05-14 | 华南理工大学 | Method for deacidizing and regenerating waste used oil by using molecular distillation technology |
| CN101319166A (en) * | 2007-10-19 | 2008-12-10 | 尹英遂 | Application of distillation and multi-stage molecular distillation technique in regeneration process for waste lubricant oil |
| CN101906348A (en) * | 2010-08-18 | 2010-12-08 | 黄卫红 | Method for reducing waste engine oil into base oil |
| CN102899124A (en) * | 2012-10-26 | 2013-01-30 | 中国石油化工股份有限公司 | Transformer oil and preparation method thereof |
| CN204073478U (en) * | 2014-08-15 | 2015-01-07 | 青岛天雄健工贸有限公司 | A kind of multiple-grade molecular distillation equipment |
| CN204891257U (en) * | 2015-08-13 | 2015-12-23 | 修武永乐新能源环保设备有限公司 | Refine waste oil recycle system of base oil |
-
2017
- 2017-11-16 CN CN201711137582.8A patent/CN107982950B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4568428A (en) * | 1983-07-05 | 1986-02-04 | General Signal Corporation | Method and apparatus for vacuum distillation |
| RU2002796C1 (en) * | 1992-01-22 | 1993-11-15 | Насир Мамед оглы Алиев | Method of transformer oil preparation |
| CN101319166A (en) * | 2007-10-19 | 2008-12-10 | 尹英遂 | Application of distillation and multi-stage molecular distillation technique in regeneration process for waste lubricant oil |
| CN101177646A (en) * | 2007-10-26 | 2008-05-14 | 华南理工大学 | Method for deacidizing and regenerating waste used oil by using molecular distillation technology |
| CN101906348A (en) * | 2010-08-18 | 2010-12-08 | 黄卫红 | Method for reducing waste engine oil into base oil |
| CN102899124A (en) * | 2012-10-26 | 2013-01-30 | 中国石油化工股份有限公司 | Transformer oil and preparation method thereof |
| CN204073478U (en) * | 2014-08-15 | 2015-01-07 | 青岛天雄健工贸有限公司 | A kind of multiple-grade molecular distillation equipment |
| CN204891257U (en) * | 2015-08-13 | 2015-12-23 | 修武永乐新能源环保设备有限公司 | Refine waste oil recycle system of base oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107982950B (en) | 2020-06-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104941383B (en) | A kind of method and device of monochloro methane tail-gas deep recovery | |
| CN103755559B (en) | A kind of method of ion liquid abstraction rectifying separation ethyl acetate-isopropanol | |
| CN105296135B (en) | A kind of regeneration method of waste lubricating oil | |
| CN103613237A (en) | Technique for processing high-salinity wastewater in preparation of hydrazine hydrate by use of ketazine process | |
| CN106698785B (en) | Coal gasification wastewater phenol-ammonia recovery process | |
| CN108299266A (en) | The preparation method of high purity N-methyl pyrrolidone | |
| CN106397252B (en) | Device and method for efficiently recycling DMF (dimethyl formamide) from wastewater | |
| CN101177646A (en) | Method for deacidizing and regenerating waste used oil by using molecular distillation technology | |
| CN105617819A (en) | Method for absorbing carbon dioxide in synthesis gas at low temperature with ionic liquid | |
| CN105754704A (en) | Method for increasing yield of base oil by adopting extracted solution for secondary extraction | |
| CN107982950A (en) | A kind of useless transformer oil recovery method | |
| EP2496328B1 (en) | Process for purifying processing fluids | |
| CN101134710A (en) | Method for reclaiming octafluorocyclobutane from residual liquid of tetrafluoroethylene manufacturing process | |
| CN107697972B (en) | Extracting agent for efficiently removing dihydric phenol in coal gasification wastewater and extracting method | |
| CN107937009A (en) | The separation method of phenolic compound in coal tar and DCL/Direct coal liquefaction product | |
| CN114772558A (en) | Process for extracting elemental sulfur from high-sulfur ore/slag | |
| CN109836304B (en) | Method for separating cyclopentane/2, 2-dimethylbutane | |
| CN219399041U (en) | Benzene and caprolactam recovery system from caprolactam benzene distillation raffinate | |
| CN104529697A (en) | Method for recovering high-purity octafluorocyclobutane from difluoromonochloro methane cracking residual liquid | |
| CN104926591B (en) | A kind of method of extracting rectifying and separating benzene and thiophene | |
| CN107573252B (en) | Method for recycling wastewater generated in process of producing glycine by chloroacetic acid method | |
| CN112979526A (en) | Preparation method of high-purity N-methyl pyrrolidone | |
| CN204476385U (en) | A kind of membrane separation process EOR extraction gas CO 2piece-rate system | |
| CN113024366B (en) | Separation method of quaternary mixture of acetone, toluene, sodium phenolate and water | |
| CN103030184A (en) | Water treatment solvent recovery method |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |