CN101619230A - Method for recycling organic compounds from caustic sludge generated in coal tar oil light end alkali cleaning - Google Patents
Method for recycling organic compounds from caustic sludge generated in coal tar oil light end alkali cleaning Download PDFInfo
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Abstract
The invention discloses a method for recycling organic compounds from the caustic sludge generated in coal tar oil light end alkali cleaning, comprising the following steps: low-boiling solvent is added in caustic sludge for extraction, the organic compounds in the caustic sludge is separated and dissolved in the low-boiling solvent, then the low-boiling solvent in extract liquor is recycled by distillation and the remainder is high concentration organic compounds. The method provided by the invention has the advantages of simple operation, low cost and no pollution.
Description
Technical field
The present invention relates to a kind of method that reclaims the alkaline residue that produces in the preparing diesel from coal tar process, be specifically related to a kind of alkaline residue that produces during with the coal tar alkali cleaning and carry out solvent extraction or extraction, to reclaim the method for organic compound in the alkaline residue.
Background technology
How to effectively utilize coal resource and make its meet environmental protection requirement, satisfy other natural resources of coal district configuration, meet this area long-run development strategy, and finally meet the research direction that national industrial policies are country, local government and enterprise always.There is a large amount of tar resources in China, how to effectively utilize coal tar and be an important step in the coal comprehensive utilization.Because petroleum resources is in short supply, more and more enterprises is making great efforts this uncleanly resource of coal tar is transformed into the cleaning alternative fuel that diesel motor can use.
Component in the coal tar is very complicated, and the main ingredient in the coal tar can be divided into aromatic hydrocarbon, phenols, heterocyclic nitrogen compounds, heterocyclic sulfur compounds, heterocycle oxygen compound and complicated polymer cyclic hydrocarbon.Comprised by lower molecular weights such as benzene and phenol, lower boiling simple material, in addition under high vacuum also not evaporable relative molecular mass reach several thousand complex compound.Its organic compound component estimates at up to ten thousand kinds, and nearly 500 kinds of certified compound contains in the coal tar above 1% component and has only 12 kinds.Therefore, the deep processing of coal tar becomes complicated unusually.
Usually, the deep processing of coal tar is to produce Chemicals such as benzene, pyridine, phenol, naphthalene with the chemical industry method, but the separation of this method or purification difficulty are bigger.For example when producing phenol, at first coal tar obtains carbolic oil through distillation, adds sodium hydroxide solution in the carbolic oil, and the phenol reaction generates phenol sodium, then phenol sodium is carried out neutralizing treatment with acid or carbon dioxide and obtains crude phenols, and phenol is purified from carbolic oil.In purification process, no matter carry out acid-base reaction and still carry out acid-base neutralisation, produce waste water essentially, the good treatment method is not found in the processing of this phenol water at present in industrial production, cause environmental pollution easily.Simultaneously, the small-sized coal tar processing enterprise that also has carries out the oil that acts as a fuel after pickling, the alkali cleaning to coal tar, has produced acid sludge and alkaline residue in process of production, also causes environmental pollution easily.In addition, refinery also has the part operation to produce alkaline residue, and the environmental protection treatment of its alkaline residue also is the technical problem that refinery is difficult to solution.
Phenolic compound is one of basic raw material of organic chemistry industry, use very extensive, as in the production of synthon, engineering plastics, medicine, agricultural chemicals, softening agent, antioxidant, dyestuff intermediate and explosive etc., being used widely.The market value of crude phenols under the not high situation of fuel oil market price, if can adopt the phenolic compound in the coal tar method of a kind of safety, environmental protection to extract, will have good market outlook more than 8000 yuan at present.
Phenolic compound has phenolic hydroxyl group, has slightly acidic, can generate sodium phenolate with alkali reaction, thereby can phenol be extracted from tarry cut with aqueous sodium hydroxide solution.The extraction of industrial crude phenols all adopts sodium hydroxide solution washing tarry cut to obtain sodium phenolate, and the sodium phenolate that is generated is dissolved in the alkali lye, owing to its density is separated greatly than distillate.
Sodium phenolate belongs to strong base-weak acid salt, in present industrial production, can it be decomposed by adopting the acid stronger than phenolic acid property, and industrial general employing sulfuric acid decomposition method and carbonic acid gas decomposition method, coal tar processing enterprise extensively adopts sulfuric acid decomposition method at present.
It is as follows that continous way sulfuric acid decomposes the technical process of phenol sodium: with clean phenol sodium and concentration is that the sulfuric acid of 40%-45% is sent into reactor simultaneously, and reaction product enters a separator after cooling.The crude phenols that reaction obtains are discharged from separator top, and metabisulfite solution is discharged in the bottom.This metabisulfite solution enters second separator, and the metabisulfite solution that contains phenol 0.4%-0.6% is discharged from the separator bottom, and crude phenols enter the crude phenols storage tank from top through regulator of level.Decompose with diluted acid, product is difficult for sulfonation, and it is not fierce to react, and decomposes fully, and smog is overflowed less, and operating environment is better.But equipment and Corrosion of Pipeline are serious, and sodium sulfate wastewater treatment difficulty, and this is the greatest problem that sulfuric acid decomposition method exists.
Patent disclosures such as Chinese invention patent CN92110407.3, CN93107496.7 a kind of method of coal tar processing oil fuel, but still adopt traditional pickling, alkaline cleaning procedure, the alkaline residue that produces in alkaline cleaning procedure is not generally processed recovery, directly uses as boiler oil.On the one hand the high added value phenolic compound in the alkaline residue is not fully utilized, the free alkali that contains in the alkaline residue will inevitably cause corrosion to boiler in combustion processes on the other hand.These patents do not have the open method that alkaline residue is recycled simultaneously.
Summary of the invention
The purpose of this invention is to provide a kind of method that reclaims the alkaline residue that produces in the preparing diesel from coal tar process, that this method has is simple to operate, cost is low, free of contamination advantage.
For achieving the above object, the present inventor has carried out a large amount of research and performing creative labour on the basis of existing technology, developed a kind of method that reclaims the alkaline residue that produces in the preparing diesel from coal tar process, it is characterized in that described method comprises the steps:
Add low boiling point solvent at alkaline residue and carry out extracting or extraction, organic compound separated and dissolved in the alkaline residue enters in the low boiling point solvent, the low boiling point solvent in extract or the extraction liquid is reclaimed in distillation then, and residuum is the organic compound of high density, is mainly phenolic compound.
Described coal tar is coalite tar, coal-tar middle oil or coal-tar heavy oil.
Described low boiling point solvent is the C in methyl alcohol, ethanol, normal hexane, normal butane, Skellysolve A, toluene, benzene, dimethylbenzene, tetrahydrofuran (THF) or the oil
4-C
5Cut.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: (10-1000), be preferably: 10: (50-200), most preferably be 10: (50-70).
Described low boiling point solvent is used for next round-robin extracting or extraction after reclaiming.
Method of returning organic compound from the alkaline residue that coal tar lighting end alkali cleaning produces provided by the invention is to add low boiling point solvent at alkaline residue to carry out extracting or extraction, organic compound separated and dissolved in the alkaline residue enters in the low boiling point solvent, the low boiling point solvent in extract or the extraction liquid is reclaimed in distillation then, residuum is the organic compound of high density, thereby realizes that valuable organic compound in the alkaline residue reclaims and the purpose of low boiling point solvent recycle.In whole process, owing to there is not the participation of water,, whole process do not produce so not having sewage, satisfied the purpose that chemical enterprise does not have " waste water " discharging; Owing to do not have carbonic acid gas and phenols steam to produce in the whole process,, satisfied the purpose that chemical enterprise does not have " waste gas " discharging so can not pollute to atmosphere; Because alkaline residue has obtained processing, so can not produce " waste residue " discharging.
Embodiment
The present invention is further illustrated below in conjunction with embodiment.
The character of the coal-tar middle oil that uses among the embodiment sees Table 1; The character of coal-tar heavy oil sees Table 2; The character of coalite tar sees Table 3;
Table 1 coal-tar middle oil property analysis
| ??C(mol％) | ??83.10 |
| ??H(mol％) | ??6.75 |
| ??O(mol％) | ??9.02 |
| ??S(mol％) | ??0.5 |
| ??N(mol％) | ??0.87 |
| Density (20 ℃, g/cm 3) | ??1.06 |
| Moisture (%) | ??4.0 |
| Ash content (%) | ??0.3 |
| Viscosity (E 80) | ??3.0 |
| Carbon residue | ??13.6 |
Table 2 coal-tar heavy oil property analysis
| Density (20 ℃, g/cm 3) | ??1.15 |
| Moisture (%) | ??＜4.0 |
| Ash content (%) | ??＜0.13 |
| Viscosity (E 80) | ??5.0 |
| Contain naphthalene amount/% | ??7.0 |
Table 3 coalite tar property analysis
| ??C(mol％) | ??84.10 |
| ??H(mol％) | ??10.35 |
| ??O(mol％) | ??4.32 |
| ??S(mol％) | ??0.31 |
| ??N(mol％) | ??0.61 |
| Density (20 ℃, g/cm 3) | ??1.008 |
| Moisture (%) | ??4.0 |
| Ash content (%) | ??0.3 |
| Viscosity (E 50) | ??3.68 |
The experimental technique of unreceipted concrete reaction conditions among the embodiment, but should be, or the condition of advising according to manufacturer according to normal condition.
The sepn process of the pre-treatment of coal tar and lighting end and last running is among the embodiment 1-6:
1. the pre-dehydration of coal tar
1000g coal tar is entered the tar storage tank through feedstock pump, temperature in storage tank (in be provided with serpentine heating pipe, pass to steam in the pipe, the storage tank shell is surrounded by thermal insulation layer to reduce heat radiation) is to leave standstill 36 hours under 85 ℃ of conditions, water separates with coal-tar middle oil, and water level is in the upper strata of coal-tar middle oil.This part water is regularly emitted along the upflow tube that has valve that the high direction of groove is installed, and the coal tar water content in oil after the pre-dehydration can reduce to about 3%.
2. the desalination of coal-tar middle oil and dehydration, take off light oil and handle
Adding concentration in the coal tar after pre-dehydration is the sodium carbonate solution of 10wt%, and yellow soda ash is 1% of coal tar weight, makes it and solid ammonium-salt generation replacement(metathesis)reaction, generates stable sodium salt.After the process filter is removed solid impurity, after being preheating to 125 ℃, coal tar enters one section evaporation element, at this, most of moisture and light oil in the coal-tar middle oil are evaporated, overflow in mixed vapour flash-pot top, obtain the phlegma of 25 ℃ of temperature through condenser, behind phase splitter, obtain one section light oil and interior ammoniated phenol water again.Light oil enters the light oil storage tank, and phenol water is discharged and entered Sewage treatment systems.Water-content in the coal tar that one section evaporation element is handled drops to below 0.5%, again it is pumped into tube furnace.
3. the separation of lighting end and alkali cleaning, pickling, alkali cleaning and refinement treatment
Coal tar is heated to temperature T through the tube furnace radiation section
4After being 400 ℃, entering flash evaporator (being the air distillation unit) and collect boiling point, obtain the 400g lighting end less than 330 ℃ lighting end.
The lighting end of collecting enters normal pressure stirring-type reactor through pump and reacts, adding mixed base A earlier under temperature is 40 ℃ reacts, react after 4 hours, stopped reaction, open the baiting valve under the reactor, pump into the standing sedimentation jar and carry out layering, supernatant liquid is collected in tundish, enter in the next normal pressure stirred autoclave through pump again, under temperature is 70 ℃, add mixing acid and react, react after 4 hours stopped reaction, open the baiting valve behind the reactor, pump into the standing sedimentation jar and carry out layering, remove the bigger acid sludge of density that dereaction produces, supernatant liquid is collected in tundish, entering normal pressure stirring-type reactor through pump again reacts, under temperature is 40 ℃, add mixed base B and react, react after 4 hours stopped reaction, open the baiting valve under the reactor, pump into the standing sedimentation jar and carry out layering, supernatant liquid is collected in tundish, obtains diesel component, the antioxidant T502 that adds its weight 0.05% makes the oxidation-resistance of diesel oil, it is stable that colourity keeps.
Described mixing acid is the mixing solutions of 30wt% sulfuric acid and 50wt% phosphoric acid, and the volume ratio of sulphuric acid soln and phosphoric acid solution is 1: 1, and its consumption is lighting end 1.5wt%.
Embodiment 1
The coal tar that uses is coal-tar middle oil;
Described mixed base A is the mixing solutions of 30wt% sodium hydroxide solution and 25wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 1, and mixed base A consumption is the 1.5wt% of lighting end;
Described mixed base B is the mixing solutions of 30wt% sodium hydroxide solution and 25wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 5, and mixed base B consumption is the 1wt% of lighting end.
Getting alkaline residue 200g packs in the cellulose thimble, carry out cable-styled extracting with the 200g benzene solvent, carry out along with extractive, phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, obtain being mixed with the solvent 240g of phenolic compound, the low boiling point solvent benzene in the extract is reclaimed in distillation, obtains reclaiming solvent benzol 180g, and remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 10.
Embodiment 2
The coal tar that uses is coal-tar middle oil;
Described mixed base A is the mixing solutions of 20wt% sodium hydroxide solution and 20wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 1, and mixed base A consumption is the 5wt% of lighting end;
Described mixed base B is the mixing solutions of 10wt% sodium hydroxide solution and 30wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 5, and mixed base B consumption is the 0.5wt% of lighting end.
Getting alkaline residue 200g packs in the cellulose thimble, carry out cable-styled extracting with 4000g normal hexane solvent, carry out along with extractive, phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, be mixed with the solvent 4195g of phenolic compound, the low boiling point solvent normal hexane in the extract is reclaimed in distillation, obtains reclaiming solvent 3990g.Remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 200.
Embodiment 3
The coal tar that uses is coalite tar;
Described mixed base A is the mixing solutions of 10wt% potassium hydroxide solution and 30wt% tetraethyl ammonium hydroxide, and the volume ratio of potassium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 1, and mixed base A consumption is the 0.5wt% of lighting end;
Described mixed base B is the mixing solutions of 15wt% sodium hydroxide solution and 20wt% triethyl, and the volume ratio of sodium hydroxide solution and triethyl solution is 100: 5, and mixed base B consumption is the 5wt% of lighting end.
Getting alkaline residue 200g packs in the cellulose thimble, extract with the 1000g tetrahydrofuran solvent, carrying out along with extraction, phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, be mixed with the solvent 1190g of phenolic compound, the low boiling point solvent tetrahydrofuran (THF) in the extraction liquid is reclaimed in distillation, obtains reclaiming solvent 995g.Remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 50.
Embodiment 4
The coal tar that uses is coal-tar heavy oil;
Described mixed base A is the mixing solutions of 15wt% sodium hydroxide solution, 10wt% potassium hydroxide solution, 25wt% tetraethyl ammonium hydroxide, the volume ratio of sodium hydroxide solution, potassium hydroxide solution and tetraethyl ammonium hydroxide solution is 50: 50: 1, and mixed base A consumption is the 3wt% of lighting end;
Described mixed base B is the mixing solutions of 20wt% sodium hydroxide solution and 25wt% triethyl, 25wt% tetraethyl ammonium hydroxide, the volume ratio of sodium hydroxide solution, triethyl solution, tetraethyl ammonium hydroxide solution is 100: 2: 3, and mixed base B consumption is the 2wt% of lighting end.
Getting alkaline residue 200g packs in the cellulose thimble, 10000g normal butane, 5000g ethanol and 5000g Skellysolve A solvent extract, carrying out along with extraction, phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, be mixed with the solvent 20190g of phenolic compound, low boiling point solvent normal butane, ethanol and the Skellysolve A in the extraction liquid reclaimed in distillation, obtains reclaiming solvent 19990g.Remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 1000.
Embodiment 5
The coal tar that uses is coal-tar middle oil;
Described mixed base A is the mixing solutions of 30wt% sodium hydroxide solution and 25wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 1, and mixed base A consumption is the 1.5wt% of lighting end;
Described mixed base B is the mixing solutions of 30wt% sodium hydroxide solution and 25wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 100: 5, and mixed base B consumption is the 1wt% of lighting end.
Get alkaline residue 200g and pack in the cellulose thimble C in 5000g toluene and the 5000g oil into
4-C
5Cut carries out cable-styled extracting, carries out along with extractive, and the phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, is mixed with the solvent 10195g of phenolic compound, low boiling point solvent toluene in the distillation recovery extract and the C in the oil
4-C
5Cut obtains reclaiming solvent 9990g.Remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 500.
Embodiment 6
The coal tar that uses is coal-tar middle oil;
Described mixed base A is the mixing solutions of 35wt% sodium hydroxide solution and 25wt% tetraethyl ammonium hydroxide, and the volume ratio of sodium hydroxide solution and tetraethyl ammonium hydroxide solution is 25: 1, and mixed base A consumption is the 1.5wt% of lighting end;
Described mixed base B is the mixing solutions of 25wt% potassium hydroxide solution and 25wt% triethyl, 25wt% tetraethyl ammonium hydroxide, the volume ratio of potassium hydroxide solution, triethyl solution, tetraethyl ammonium hydroxide solution is 100: 3: 2, and mixed base B consumption is the 4wt% of lighting end.
Getting alkaline residue 200g packs in the cellulose thimble, 1000g methyl alcohol and 400g xylene solvent carry out cable-styled extracting, carry out along with extractive, phenolic compound in the cellulose thimble is come out to enter into solvent by solvent extraction, be mixed with the solvent 1590g of phenolic compound, low boiling point solvent methyl alcohol and the dimethylbenzene in the extract is reclaimed in distillation, obtains reclaiming solvent 1387g.Remaining product is the crude phenols compounds of retrieving in the alkaline residue.
The weight part ratio of described alkaline residue and low boiling point solvent is 10: 70.
Claims (8)
1. a method that reclaims organic compound from the alkaline residue that coal tar lighting end alkali cleaning produces is characterized in that described method comprises the steps:
Add low boiling point solvent and carry out extracting or extraction in alkaline residue, the organic compound separated and dissolved in the alkaline residue enters in the low boiling point solvent, and the low boiling point solvent in extract or the extraction liquid is reclaimed in distillation then, and residuum is the organic compound of high density.
2. method according to claim 1 is characterized in that described coal tar is coalite tar, coal-tar middle oil or coal-tar heavy oil.
3. method according to claim 1 is characterized in that described low boiling point solvent is the C4-C5 cut in methyl alcohol, ethanol, normal hexane, normal butane, Skellysolve A, toluene, benzene, dimethylbenzene, tetrahydrofuran (THF) or the oil.
4. method according to claim 1, the weight part ratio that it is characterized in that described alkaline residue and low boiling point solvent is 10: (10-1000).
5. method according to claim 4, the weight part ratio that it is characterized in that described alkaline residue and low boiling point solvent is 10: (50-200).
6. method according to claim 5, the weight part ratio that it is characterized in that described alkaline residue and low boiling point solvent is 10: (50-70).
7. method according to claim 6 is characterized in that being used for next round-robin extracting or extraction after described low boiling point solvent reclaims.
8. method according to claim 1 is characterized in that described organic compound is a phenolic compound.
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| CN102719267A (en) * | 2012-06-28 | 2012-10-10 | 神华集团有限责任公司 | Separation method for phenolic compound in coal liquefied oil |
| CN105018124A (en) * | 2015-07-15 | 2015-11-04 | 太原市金浦顺化工有限公司 | Coal tar waste-residue extraction separation method |
| CN105013800A (en) * | 2015-07-15 | 2015-11-04 | 太原理工大学 | Method for recovering composite extracting agent in extraction and separation process of coal tar waste residues |
| CN105176557A (en) * | 2015-08-21 | 2015-12-23 | 长岭炼化岳阳工程设计有限公司 | Device and method for desalting coal tar and recovering phenol |
| CN106635144A (en) * | 2016-11-23 | 2017-05-10 | 辽宁石油化工大学 | Method for enriching and separating phenolic compounds in shale oil |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102719267A (en) * | 2012-06-28 | 2012-10-10 | 神华集团有限责任公司 | Separation method for phenolic compound in coal liquefied oil |
| CN105018124A (en) * | 2015-07-15 | 2015-11-04 | 太原市金浦顺化工有限公司 | Coal tar waste-residue extraction separation method |
| CN105013800A (en) * | 2015-07-15 | 2015-11-04 | 太原理工大学 | Method for recovering composite extracting agent in extraction and separation process of coal tar waste residues |
| CN105013800B (en) * | 2015-07-15 | 2017-04-19 | 太原理工大学 | Method for recovering composite extracting agent in extraction and separation process of coal tar waste residues |
| CN105176557A (en) * | 2015-08-21 | 2015-12-23 | 长岭炼化岳阳工程设计有限公司 | Device and method for desalting coal tar and recovering phenol |
| CN106635144A (en) * | 2016-11-23 | 2017-05-10 | 辽宁石油化工大学 | Method for enriching and separating phenolic compounds in shale oil |
| CN106635144B (en) * | 2016-11-23 | 2018-05-04 | 辽宁石油化工大学 | A kind of method of phenolic compound concentration and separation in shale oil |
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Application publication date: 20100106 |