CN105368580A - Organic chloride removing method for waste cooking oil - Google Patents
Organic chloride removing method for waste cooking oil Download PDFInfo
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Abstract
The invention discloses an organic chloride removing method for waste cooking oil. The organic chloride removing method aims at eliminating the harm of organic chloride to subsequent processing equipment and comprises the steps that at least one stage of electric desalting is conducted on the waste cooking oil; then 6-15% by weight of water is added into the waste cooking oil subjected to electric desalting to be mixed with the oil, and a dechlorination agent is added to perform dechlorination reaction, wherein the dechlorination reaction conditions are described as: the reaction temperature is 90-150 DEG C, the reaction time is 45-120 minutes, the stirring rate is 100-600 r/min, and the agent-chlorine mass ratio is 2-20:1 generally; a reaction product obtained after dechlorination reaction is subjected to electric desalting again to obtain organic chlorine removed cooking oil. The organic chloride in waste cooking oil can be efficiently removed by using the method at low cost.
Description
Technical field
The invention belongs to the pretreatment technology of the remaining waste oil of meal (be commonly called as " sewer oil "), particularly a kind of waste cooking oil is as the organochlorine removal methods of biology boat coal stock oil processing.
Background technology
Progressively decline at fossil fuel reserves, under background that environment protection is increasingly serious, biofuel is a kind of novel energy of alternative fossil energy, and its investigation and application more and more comes into one's own.
Biological boat coal take renewable resources as the aviation kerosene of raw material production, and compared with conventional petroleum base aviation kerosene, biological boat coal can realize reducing emission of carbon dioxide more than 55%, and can regenerate, and has sustainability, has very high environment-friendly advantage.Comparatively early, development is very fast, and American-European major country carried out research and development and the test of bio-aviation fuel successively from 2008, within 2011, rose and started to carry out comercial operation for the starting of foreign biomolecule boat coal technology.
The successful experience of foreign biomolecule diesel oil and maturation process are that the development of China's biofuel industry provides beneficial reference, but foreign biomolecule diesel raw material is mostly rapeseed oil and soybean oil, source is simple, material quality is better, impurity element is as very low in organochlorine and free acid content, does not substantially need the imurity-removal pre-treatment carrying out raw material, and production and processing process is relatively short simultaneously, raw material corrosion is slight, requires lower to anticorrosion aspect.China's edible oil external dependence degree is more than 60%, available vegetable oil resource is deficient, waste grease be current we develop the important source material foothold of biofuel, wherein major part is waste cooking oil, in view of its source is complicated, collection method is different, and foreign matter content is different with type, especially containing a large amount of salt, free fatty acids, organic chloride, raw material organochlorine is removed, electric desalting and following process protection against corrosion propose an urgent demand.Especially along with China's the Implement of sustainable development strategy, policy inclination is carried out to biofuel development, biofuel industry has development potentiality, therefore for these to the outstanding and in the urgent need to address problem faced in the biofuel course of processing, domestic have very big market.
Biological boat coal raw material mainly relies on waste animal and vegetable oil, wherein major part is waste cooking oil " sewer oil ", this is for solution sewer oil backflow dining table, reduce domestic food potential safety hazard significant, but because raw material sources are complicated, recovery process is different, nature difference is larger, see with regard to current result of study, the waste cooking oil cl content in different batches and source is higher, and (total chlorine is up to more than 20mg/l, and the overwhelming majority is organochlorine), free fatty acid content high (acid number is the highest more than 40mgKOH/g), water-content is high, and in emulsified state, the production technique of biological boat coal cannot be directly used in.
Owing to containing a large amount of free fatty acids in waste cooking oil, heavy corrosion can be caused to system device and pipeline before hydrotreatment, navigate in the follow-up hydrogenation process of coal raw material at waste cooking oil as biology, the a large amount of inorganic chlorines, organochlorine and the small molecular organic acid that contain in waste cooking oil raw material can produce serious low temperature corrosion and high temperature corrosion to relevant device and pipeline, and therefore the biological etching problem navigated in coal raw materials pretreatment and following process process is also the aspect needing to pay close attention to.
Waste cooking oil is still immature at present as the pretreatment technology of biology boat coal raw material, although existing technology of electric de-salting can remove wherein most of inorganic chlorine, however very low to the organochlorine decreasing ratio in raw material.Residual chlorine after desalination, major part exists with organochlorine form, can decompose generation hydrogenchloride in follow-up hydrogenation process, owing to there being water to generate in hydrogenation process, can forming strongly-acid corrosive environment, do great damage to equipment installation at topical hypothermia position.
How to remove the organochlorine in waste cooking oil, be a technical problem urgently to be resolved hurrily high efficiency, low cost.Therefore, the necessary organochlorine carrying out waste cooking oil removes research, to form the biology boat coal raw material pretreatment process system of stability and high efficiency, guarantees the smooth running of follow-up hydrogenation technique.
Summary of the invention
The object of this invention is to provide a kind of organochlorine removal methods of waste cooking oil.With to the organochlorine in waste cooking oil, by a kind of high performance dechloridizing agent, use the combination of chemical reaction dechlorination and electric desalting dechlorination, solve the harm that organochlorine causes following process device.Use the inventive method can remove the organochlorine in waste cooking oil high efficiency, low cost.
The invention provides a kind of organochlorine removal methods of waste cooking oil, it is characterized in that comprising the steps:
1) waste cooking oil is carried out to the electric desalting of at least one-level, water injection rate during electric desalting is 6 ~ 15 % by weight of waste cooking oil gross weight;
2) in the waste cooking oil after electric desalting, add 6 ~ 15 % by weight water mixing, the water yield added, with the waste cooking oil total weight after electric desalting, adds dechlorinating agent afterwards and carries out dechlorination reaction;
Described dechlorination reaction condition is: temperature of reaction 90 ~ 150 DEG C, reaction times: 45 ~ 120min, stir speed (S.S.): 100 ~ 600r/min, dechlorinating agent consumption according to raw material (namely electric desalting and after adding water waste cooking oil) in cl content and determine, agent chlorine mass ratio is generally 2 ~ 20: 1, agent chlorine mass ratio be the quality of dechlorinating agent and raw material (namely electric desalting and after adding water waste cooking oil) in the ratio of the quality of chlorine that contains;
3) reaction product after dechlorination reaction carries out electric desalting again, and water injection rate is 6 ~ 15 % by weight of reaction product gross weight after dechlorination reaction.
The further technical characteristic of the inventive method is: described electric desalting condition is: strength of electric field 800 ~ 1500V/cm, mixture strength: 100 ~ 500 times hand, electric desalting time: 15 ~ 60min, electric desalting temperature: 90 ~ 150 DEG C.
The further technical characteristic of the inventive method is: described dechlorinating agent is made up of following component:
(A) organochlorine transforming agent, 30 ~ 80%;
(B) organochlorine transfer agent, 5 ~ 40%;
(C) auxiliary agent, 5 ~ 40%.
With dechlorinating agent total weight.
Wherein component (A) organochlorine transforming agent is nucleophilic reagent, be mainly one or more mixtures in the metal-salt of alcohol, alkali-metal oxyhydroxide and carboxylate salt, one or more mixtures in particular methanol potassium, potassium ethylate, sodium ethylate, sodium methylate, potassium isopropoxide, potassium tert.-butoxide, sodium hydroxide, potassium hydroxide, sodium formiate and sodium acetate;
Component (B) organochlorine transfer agent is consisting of phase-transferring agent, there is oil soluble and water-soluble dual nature, be mainly quaternary ammonium hydroxide, quaternary ammonium salt or season phosphonium salt, preferred trimethyl benzyl ammonium hydroxide, tetrabutylammonium hydroxide amine, triethylbenzyl ammonium hydroxide, hydroxide beta-hydroxyethyl Trimethylamine 99, tricaprylmethyl ammonium hydroxide, tetra-n-butyl Ammonium hydrogen sulfate, tributyl hexadecyl bromide phosphine or ethyltriphenylphosphonium bromide;
Component auxiliary agent (C) solvent can be one or more mixtures in glycerol, Virahol, ethanol, methyl alcohol, hexanol, dimethyl sulfoxide (DMSO) and dimethyl formamide.
Electric desalting of the present invention adopts the method for conventional electric desalting, most of inorganic chlorine can be removed, and remaining is all organochlorine.
The principle of the inventive method is: be mainly divided into two processes, and chemical reaction realizes organochlorine and transforms to the transfer of inorganic chlorine, and technology of electric de-salting realizes removing of inorganic chlorine.Organochlorine subtractive process, mainly follow phase transition acceleration nucleophilic substitution reaction to have come, under condition of phase transition, organochlorine changes into inorganic chlorine, and inorganic chlorine enters aqueous phase under consisting of phase-transferring agent carries, and reacts with nucleophilic reagent, generate metal chloride, and consisting of phase-transferring agent is reduced, catalytic cycle reaction can be continued, until organochlorine is converted into inorganic chlorine completely.After reaction terminates, thoroughly remove inorganic chlorine by the technology of electric de-salting optimized.Concrete reaction process is shown below.
Above formula is that the theoretical formula of dechlorination reaction is accelerated in phase transition.
Wherein: Q+---the positive ion Nu of consisting of phase-transferring agent
----nucleophilic reagent negative ion
QNu---carries the ion pair RCl of nucleophilic reagent---organic chloride
RNu---reaction product QCl---consisting of phase-transferring agent ion pair
The inventive method compared with prior art has following advantage:
1) the inventive method adopts phase transfer catalytic technology, under liquid-phase condition, organic chloride is converted into inorganic chlorine, and remove in conjunction with technology of electric de-salting, speed of reaction can be improved rapidly, improve dechlorination effect, thus avoid waste cooking oil as the harm that during biology boat coal raw material, these muriates cause in following process process.
2) the inventive method is for organic chloride in waste cooking oil, chemical reaction dechlorination and technology of electric de-salting are organically combined, solve the problem of waste cooking oil as organochlorine corrosion in biology boat coal raw material, and be that waste cooking oil provides counte-rplan as raw materials pretreatment during biology boat coal raw material.
3) the inventive method is by the organochlorine removal methods of efficient quick, reduce content of organic chloride in waste cooking oil, salts contg and water-content, both improve the raw materials quality of biological boat coal processing, alleviate equipment corrosion again, improve the work-ing life of device, thus improve the economic benefit of biological boat coal processing.Meanwhile, the method has widened the source of biological boat coal raw material, solves the problem of waste cooking oil and sewer oil backflow dining table, avoids the pollution of sewer oil to environment, economize on resources.
4) the inventive method is applied widely, and working conditions is not harsh, and cost is lower, handled easily, practical reliable, does not need to increase expensive hydrogenation unit and dechlorination apparatus.This dechlorination method to existing production unit and operational condition without the need to changing, simple possible.
Below in conjunction with specific embodiment, the present invention is described in further detail, but these embodiments are not for limiting the scope of the invention by any way.
Embodiment
Embodiment 1 ~ 4 is shown in dechlorination effect evaluation;
Embodiment 1
Prepared by base oil: after waste cooking oil raw material being carried out continuously three pro desalting dehydrations, obtained base oil.Employing base oil is tested, and fully can eliminate the impact of inorganic chlorine, the more convenient effect of proof test quickly.
Pro desalting dehydration test condition: temperature 90 DEG C, strength of electric field 1300V/cm, water filling 12wt%, rock 200 times, residence time 30min.Three grades of pro desalting, every grade of pro desalting condition is all identical.
Consider that in base oil, content of inorganic chlorine is very low, set remaining whole be organochlorine, its total chlorine m of analyzing and testing
0for 17ppm.Dechlorination reaction and electricity are got upper strata oil sample respectively, lower floor's water sample are carried out saliferous, bearing analysis, get upper strata oil sample in addition again and carry out total chlorine analysis, consider that total chlorine of analyzing and testing all can regard as organochlorine after taking off and terminating.Be calculated as follows organochlorine decreasing ratio:
T’＝(m
0-m
1)*100％/m
0
In formula: T '-organochlorine decreasing ratio
M
0the content of organic chloride of-base oil, ppm
M
1after-dechlorination reaction and electric desalting terminate, the content of organic chloride in test oil sample, ppm
Adopt base oil to carry out dechlorination experiment, water filling 15 % by weight in base oil, then add each component A of dechlorinating agent, B, C carry out dechlorination reaction, after reaction terminates, adopt YS-3 electric desalting instrument, carry out high-temperature electric desalination test, A is organochlorine transforming agent, and B is organochlorine transfer agent, and C is auxiliary agent.
Dechlorination reaction condition: oil based on 0#, 1#, 2# do not participate in reaction, directly carry out electric desalting, 3 ~ 7# water filling, add dechlorinating agent, participate in dechlorination reaction, temperature of reaction: 90 DEG C, in the reaction times: 45min, stir speed (S.S.): 400r/min, carries out electric desalting test after reaction terminates.
The dechlorinating agent 170ppm that 3#, 4#, 5#, 6#, 7# annotate dissimilar respectively, agent chlorine ratio (mass ratio)=10: 1 is below the concrete proportion of composing of dechlorinating agent:
3# dechlorinating agent component is: A sodium ethylate 70%wt, B benzyltrimethylammonium hydroxide 20%wt, C glycerol 10%wt;
4# dechlorinating agent component is: A sodium ethylate 70%wt, B TBAH 20%wt, C glycerol 10%wt:
5# dechlorinating agent component is: A sodium ethylate 70%wt, B 4-butyl ammonium hydrogen sulfate 20%wt, C glycerol 10%wt:
6# dechlorinating agent component is: A sodium ethylate 70%wt, B tricaprylmethyl oxyammonia 20%wt, C glycerol 10%wt;
7# dechlorinating agent component is: A sodium ethylate 70%wt, B hydroxide beta-hydroxyethyl Trimethylamine 99 20%wt, C glycerol 10%wt;
Electric desalting test conditions: temperature 90 DEG C, strength of electric field 1300V/cm, water filling 15wt%, rock 200 times, and residence time 30min, test-results is in table 1.
The different organochlorine transfer agent of table 1 is on the impact of dechlorination effect
From table 1 test-results, in base oil, inorganic salt are easy to remove, but organochlorine relies on separately technology of electric de-salting to be difficult to remove.Adopt self-assembly electric desalting easy device, after carrying out three grades of electric desalting of waste cooking oil, obtained base oil 0#, its salts contg has taken off to 2.3mg/L (stock oil saliferous 12mg/L), and chloride content is still up to 17ppm (stock oil chloride content is 23ppm).Blank test 1#, 2# get base oil and re-inject 15% water, and after one-level electric desalting, its salts contg is minimum to be taken off to 1.0mg/L, but content of organic chloride is still up to 17ppm, if without dechlorination reaction, directly carry out electric desalting, decreasing ratio be there is no to organochlorine.
In addition, in blank test, water-content still exceedes the moisture index of electric desalting 0.3%, illustrates that this biology boat coal raw material is easily hydrolyzed, emulsification, dewaters more difficult.
1#, 2# do not participate in reaction, directly carry out one-level electric desalting, in water, saliferous is 2mg/L, by contrast, 3 ~ 7# is after first order reaction, one-level electric desalting, and in water, saliferous is sharply increased to 50mg/L, as can be seen here, after adding dechlorinating agent, organochlorine changes into inorganic chlorine, and dechlorination and desalting effect are significantly improved.From the actual detected result of organochlorine, after adding dechlorinating agent, the actual decreasing ratio of organochlorine is all more than 50%, in electric desalting draining, not only there is a large amount of inorganic chlorines to remove, and there is a part of transition state chlorine, be i.e. the organochlorine of Partial Conversion, be in metastable state, be dissolvable in water in water and remove.
From table 1, compare under the same terms, because the active ingredient of dechlorinating agent is different, namely when organochlorine transforming agent, auxiliary agent are identical, different transfer agents, transfer activity for chlorine is different, there is certain difference in dechlorination effect, adopt benzyl tribenzyl trimethylammonium hydroxide as organochlorine transfer agent, can obtain good dechlorination effect, under A (sodium ethylate)-B (benzyltrimethylammonium hydroxide)-C (glycerol) compound system, organochlorine decreasing ratio is up to 60%.
Embodiment 2
With benzyltrimethylammonium hydroxide as organochlorine transfer agent B, base oil used is identical with embodiment 1, select dissimilar organochlorine transforming agent A, auxiliary agent C and B benzyltrimethylammonium hydroxide composite, add dosage and remain unchanged, still be 170ppm, agent chlorine ratio (mass ratio)=10: 1, operation steps is identical with embodiment 1, and other processing condition are constant, investigate dissimilar organochlorine transforming agent A to the impact of dechlorination, experimental result is in table 2.
Dechlorinating agent adds each component ratio:
1# dechlorinating agent component is: A sodium ethylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C glycerol 10%wt;
2# dechlorinating agent component is: A sodium methylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C glycerol 10%wt;
3# dechlorinating agent component is: A potassium ethylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C glycerol 10%wt;
4# dechlorinating agent component is: A potassium methylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C glycerol 10%wt;
5# dechlorinating agent component is: A potassium methylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C dimethyl formamide 10%wt;
6# dechlorinating agent component is: A potassium methylate 70%wt, B benzyltrimethylammonium hydroxide 20wt%, C dimethyl sulfoxide (DMSO) 10%wt;
Active and the effect of the dechlorination of different compound system from table 2, optimized compound system is: A (potassium methylate)-B (benzyltrimethylammonium hydroxide)-C (glycerol), and its organochlorine decreasing ratio is up to 75%.In view of this, there is marked difference in reactive behavior and the nucleophilic performance of transforming agent, and the active order of transforming agent is: potassium methylate > potassium ethylate > sodium methylate > sodium ethylate; Suitable auxiliary agent can provide good reaction conditions, and promote organochlorine and transforming agent, fully the contacting of transfer agent, the facilitation effect of auxiliary agent is obviously different, and glycerol optimum, dimethyl formamide takes second place, and dimethyl sulfoxide (DMSO) effect is the poorest.
The different organochlorine transforming agent of table 2, auxiliary agent are on the impact of dechlorination effect
Embodiment 3
Adopt A (potassium methylate)-B (benzyltrimethylammonium hydroxide)-C (glycerol) as compound system, change the ratio of A, B, operation steps is identical with embodiment 2, and the ratio of A, B of investigating is on the impact of dechlorination, and experimental result is in table 3.Electric desalting condition and above-described embodiment 1,2 identical.Base oil used is identical with embodiment 1.
Dechlorinating agent adds consumption and is 170ppm, and agent chlorine ratio (mass ratio) is 10: 1, and each component ratio of the dechlorinating agent added is respectively:
1#A potassium methylate 70%wt, B benzyltrimethylammonium hydroxide 20%wt, C glycerol 10%wt;
2#A potassium methylate 65%wt, B benzyltrimethylammonium hydroxide 25%wt, C glycerol 10%wt;
3#A potassium methylate 60%wt, B benzyltrimethylammonium hydroxide 30%wt, C glycerol 10%wt;
4#A potassium methylate 55%wt, B benzyltrimethylammonium hydroxide 35%wt, C glycerol 10%wt;
5#A potassium methylate 50%wt, B benzyltrimethylammonium hydroxide 40%wt, C glycerol 10%wt;
From table 3, along with the increase of the ratio of organochlorine transfer agent, organochlorine decreasing ratio raises gradually, and after organochlorine transfer agent content reaches 30%wt, organochlorine decreasing ratio substantially no longer increases, and now decreasing ratio is 81%; Using A (potassium methylate)-B (benzyltrimethylammonium hydroxide)-C (glycerol) as compound system agent, it is composite that it forms proportionally 60%wt, 30%wt, 10%wt, just can obtain reasonable dechlorination effect, this illustrates this dechlorinating agent excellent property, and compounded combination can play synergistic function.
In addition, along with the increase of the ratio of organochlorine transfer agent and the adjusting and optimizing of processing condition, in water, salts contg also presents certain increasing trend, this illustrates that the decreasing ratio of salts contg and organochlorine in water exists certain funtcional relationship, but might not be linear relationship, can judge substantially, in water, salts contg be higher, the organochlorine total amount removed is larger, and the actual decreasing ratio of corresponding organochlorine is higher.After dechlorination transfer conversion reaction, really there is a part of organochlorine being in criticality and be removed totally.
Different A, B consumption of table 3 is on the impact of dechlorination effect
Embodiment 4
On the basis of embodiment 2,3, improving technique condition.Change temperature of reaction, observing response temperature is on the impact of dechlorination effect.Still select A (potassium methylate 60%wt)-B (benzyltrimethylammonium hydroxide 30%wt)-C (glycerol 10%wt) as compound system.Electric desalting condition remains unchanged, and experimental result is in table 4.
1#, 2#, 3#, 4#, temperature of reaction is followed successively by: 90 DEG C, 110 DEG C, 130 DEG C, 150 DEG C, and in the reaction times: 1h, stir speed (S.S.): 400r/min, adds dosage: 170ppm, and agent chlorine ratio is 10: 1.
Data from table 4, after improving technique condition, the decreasing ratio of organochlorine can be stabilized in more than 80% substantially.Under these processing condition, the rising of temperature of reaction is little on dechlorination effect impact, and this may be adding due to phase-transfer catalyst, fully can reduce reaction activity, thus makes organochlorine under cryogenic, just can with nucleophilic reagent generation chemical reaction.Obviously, the impact of change on water-content of processing condition is little.
As can be seen here, after adjusting process project, the actual decreasing ratio of organochlorine is up to 84%.This absolutely proves: adding dechlorinating agent in stock oil fully can improve dechlorination effect, its process is: in oil phase-aqueous phase two-phase system, transfer agent has oil soluble and water-soluble dual nature, organochlorine transfer agent B elder generation and organochlorine generation nucleophilic substitution reaction, generate the muriate of transition state, then again there is nucleophilic substitution reaction with transforming agent A, generate butter, transfer agent reduces, again enter oil phase and continue circulating reaction, the inorganic chlorine that in aqueous phase system, solubilized is a large amount of and the muriate of transition state, the technology of electric de-salting that employing is optimized and revised can by inorganic chlorine, transition state chlorine thoroughly removes.
Organochlorine removal effect: total chlorine of base oil is down to 2 ~ 3ppm, exclude instrument blank and noise jamming, organochlorine decreasing ratio is up to 84%, and de-rear saliferous < 2mg/L, moisture < 0.5%, can meet advanced desalination dehydration indexes.
Table 4 differential responses temperature is on the impact of dechlorination effect
Claims (5)
1. an organochlorine removal methods for waste cooking oil, is characterized in that comprising the steps:
1) waste cooking oil is carried out to the electric desalting of at least one-level, water injection rate during electric desalting is 6 ~ 15 % by weight of waste cooking oil gross weight;
2) in the waste cooking oil after electric desalting, add 6 ~ 15 % by weight water mixing, the water yield added, with the waste cooking oil total weight after electric desalting, adds dechlorinating agent afterwards and carries out dechlorination reaction; Described dechlorination reaction condition is: temperature of reaction 90 ~ 150 DEG C, the reaction times: 45 ~ 120min, stir speed (S.S.): 100 ~ 600r/min, and the ratio of the quality of the chlorine contained in the quality of dechlorinating agent and electric desalting and the waste cooking oil after adding water is 2 ~ 20: 1;
3) reaction product after dechlorination reaction carries out electric desalting again, and water injection rate is 6 ~ 15 % by weight of reaction product gross weight after dechlorination reaction.
2. the organochlorine removal methods of a kind of waste cooking oil according to claim 1, it is characterized in that: described electric desalting condition is: strength of electric field 800 ~ 1500V/cm, mixture strength: 100 ~ 500 times are hand, electric desalting time: 15 ~ 60min, electric desalting temperature: 90 ~ 150 DEG C.
3. the organochlorine removal methods of a kind of waste cooking oil according to claim 1, is characterized in that: described dechlorinating agent is made up of following component:
(A) organochlorine transforming agent, 30 ~ 80%;
(B) organochlorine transfer agent, 5 ~ 40%;
(C) auxiliary agent, 5 ~ 40%.
With dechlorinating agent total weight;
Wherein component (A) organochlorine transforming agent is one or more mixtures in the metal-salt of alcohol, alkali-metal oxyhydroxide and carboxylate salt;
Component (B) organochlorine transfer agent be quaternary ammonium hydroxide, quaternary ammonium salt or season phosphonium salt;
Component auxiliary agent (C) solvent is one or more mixtures in glycerol, Virahol, ethanol, methyl alcohol, hexanol, dimethyl sulfoxide (DMSO) and dimethyl formamide.
4. the organochlorine removal methods of a kind of waste cooking oil according to claim 3, is characterized in that: described component (A) organochlorine transforming agent is one or more mixtures in potassium methylate, potassium ethylate, sodium ethylate, sodium methylate, potassium isopropoxide, potassium tert.-butoxide, sodium hydroxide, potassium hydroxide, sodium formiate and sodium acetate.
5. the organochlorine removal methods of a kind of waste cooking oil according to claim 3, is characterized in that: described component (B) organochlorine transfer agent is trimethyl benzyl ammonium hydroxide, tetrabutylammonium hydroxide amine, triethylbenzyl ammonium hydroxide, hydroxide beta-hydroxyethyl Trimethylamine 99, tricaprylmethyl ammonium hydroxide, tetra-n-butyl Ammonium hydrogen sulfate, tributyl hexadecyl bromide phosphine or ethyltriphenylphosphonium bromide.
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| CN112920842A (en) * | 2019-12-05 | 2021-06-08 | 武汉科林化工集团有限公司 | Method for removing organic chlorine in waste lubricating oil |
| US11466230B1 (en) | 2021-05-20 | 2022-10-11 | Chevron U.S.A. Inc. | Removing organic chlorides from glyceride oils |
| WO2022243760A1 (en) * | 2021-05-20 | 2022-11-24 | Chevron U.S.A. Inc. | Removing organic chlorides from glyceride oils |
| WO2023187628A3 (en) * | 2022-03-31 | 2023-12-07 | Technoilogy S.R.L. | Process for removing organic chlorine from used cooking oils (uco), animal and vegetable recovery fats (avr), and pyrolysis oils (po) derived from waste |
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