CN105112084A - Device and method for extracting phenol products from medium-low temperature coal tar - Google Patents
Device and method for extracting phenol products from medium-low temperature coal tar Download PDFInfo
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Abstract
The invention provides a device and method for extracting phenol products from medium-low temperature coal tar. The device comprises extractors, a first distiller, a second distiller, a first extraction agent storage tank, a second extraction agent storage tank and a second extraction agent adjusting tank. The multiple extractors are connected in series, raffinate of at least the last extractor enters the second extraction agent adjusting tank to guarantee the usage quantity of second extraction agents in the first extractor, and extract phases of the last extractor enter the first extraction agent storage tank after being distilled. Extract phases of each extractor except the last extractor enter the next extractor, raffinate enters the second extraction agent storage tank after being distilled, and an outlet of the second extraction agent storage tank is connected with inlets of all the extractors except the first extractor. The extraction agents are used for repeated extraction, in this way, the content of neutral oil in impurities in the extract phases can be reduced, through three times of extraction, the relative purity of phenols can reach over 97%, and through five times of extraction, the relative purity of crude phenols can be higher.
Description
[technical field]
The invention belongs to coal chemical technology, specifically a kind of extraction process extract in the technique of coalite tar phenolic compound.
[background technology]
Phenolic compound is important industrial chemicals and the intermediate of medicine, agricultural chemicals, oxidation inhibitor etc., separating phenols compounds from coal derived liquid, except the association problem of coal derived liquid can be solved, reduce the hydrogen-consuming volume of the course of processing, in the work-ing life etc. of extending catalyst, the fine chemicals of high added value can also be obtained.
What current research was more carry phenol method mainly contains chemical method and selective solvent extraction process.Chemical method is mainly with alkali cleaning dephenolize method separation and Extraction phenolic compound.It is lower to there is dephenolize rate in the method, and alkali acid consumption is large, and washing steps is many, and the time is long, and energy consumption is high, and polyphenol and higher phenols difficulty reclaim, and are particularly easy to cause the disadvantages such as the oxidizable loss of phenols.Selective solvent extraction process mainly contains superheated water extraction process, salts solution extraction process, alcohol solution extraction process, this method complex technical process, and phenols percentage extraction is lower, and commercial viability is not high.
In addition, coking field also has extraction to put forward phenol technique, and its technical scheme is: in thing to be extracted, add extraction agent, carries out phenol removal, is extracted agent-phenol and dephenolize tar.But due to the boiling point of aldehydes matter and extraction agent boiling point closely, by distil process, phenol cannot be separated with extraction agent.General way is: in aldehydes matter and extraction agent, add another reverse-extraction agent, obtains reverse-extraction agent-phenol and extraction agent, then is separated with phenol by reverse-extraction agent.But, because extraction agent and phenol have good intermiscibility, after adding reverse-extraction agent, still can mix in extraction agent and have certain aldehydes matter, like this, when after extraction agent circulation several times, the efficiency of this extraction agent will be very low, finally cause using, must extraction agent be changed, also can cause the loss of aldehydes matter simultaneously.
[summary of the invention]
In order to the extraction problem of phenolic compound in coalite tar in solving, the invention provides device and extracting method that phenolic product is put forward in a kind of middle coalite tar extraction.
The present invention is by the following technical solutions:
The device of phenolic product is carried in a kind of middle coalite tar extraction, comprise extractor and separator, extractor is L and is connected in series, wherein, the extraction phase of upper level extractor enters into next stage extractor, the extraction phase of most end one-level extractor, after 1# separator is separated, obtains crude phenols product and 1# extraction agent, and the 1# extraction agent separated provides extraction agent for first step extractor; The equal direct circulation reuse of extracting phase of most end m extractor provides 2# extraction agent for 1# extractor, the extracting phase of other extractor is after 2# separator is separated, obtain dephenolize oil and 2# extraction agent, wherein, the consumption of the 2# extraction agent of value required for first step extractor of m is determined, m=1 ~ L-1.
The 2# extraction agent source line of other extractors except first step extractor is provided with 2# extraction agent adjustment entrance, to adjust consumption and the proportioning of 2# extraction agent.
The 1# extraction agent source line of described first step extractor is provided with 1# extraction agent adjustment entrance, to adjust consumption and the proportioning of 1# extraction agent.
The device that phenolic product is put forward in described middle coalite tar extraction includes 2# extraction agent surge tank further, the entrance of this 2# extraction agent surge tank is connected with the extracting phase of m extractor of most end, and the outlet of this 2# extraction agent surge tank is connected with the 2# extraction agent entrance of 1# extractor.
The device that phenolic product is put forward in described middle coalite tar extraction comprises 1# extraction agent storage tank and 2# extraction agent storage tank further, the 1# extraction agent that most end one-level extractor is separated is stored in 1# extraction agent storage tank, the extracting phase of other extractors except most end m extractor is after being separated, and the 2# extraction agent obtained is stored in 2# extraction agent storage tank.
Described 2# extraction agent storage tank is provided with alternate outlets and is connected with the entrance of first step extractor; Described 2# extraction agent surge tank is provided with alternate outlets, and this alternate outlets is connected with the entrance of 2# separator; When the contaminant overstandard of extraction agent in 2# extraction agent surge tank, respective alternate outlets enabled respectively by 2# extraction agent surge tank and 2# extraction agent storage tank.
The device that phenolic product is put forward in described middle coalite tar extraction includes 0# separator further, and coal tar is after this 0# separator is separated, and the coal tar obtained is connected with first step extractor entrance containing the outlet of phenol fraction section, remainingly enters 0# storage tank mutually.
The outlet line of 1# extraction agent storage tank and 2# extraction agent storage tank is respectively arranged with extractant concentration proofing unit, according to detected result by reserved mouth for subsequent use, Solvent quantity and proportioning in adjustment storage tank; The outlet line of described 2# extraction agent surge tank is provided with impurity detection device, if detected result display impurity content exceeding index, then close the Trunk Line at proofing unit place, start active redundancy pipeline, comprise 2# extraction agent surge tank to the active redundancy pipeline of 2# separator and 2# extraction agent storage tank to the active redundancy pipeline of 1# extractor.
A method for phenolic product is put forward in middle coalite tar extraction, and this device putting forward phenolic product comprises L extractor and 1# and 2# separator, wherein, is connected in series between L extractor; Specifically comprise the following steps:
(1) after 1#, 2# two kinds of extraction agents and coal tar fraction section carry out extraction process in first step extractor, the extraction phase of lower floor enters into the extractor of next stage, and the extracting phase on upper strata, after 2# separator is separated, obtains 2# extraction agent and dephenolize oil;
(2) extract successively under the effect of the extraction phase that provides at upper level extractor successively of second stage extractor and n extractor being connected in series with it and 2# extraction agent, after having extracted, the extracting phase on upper strata is separated through 2# separator, obtain 2# extraction agent and dephenolize oil, the extraction phase of lower floor enters into next stage extractor;
(3) extract successively under the effect of the extraction phase that m the extractor being positioned at most end provides at upper level extractor and 2# extraction agent, after having extracted, the extracting phase on upper strata provides 2# extraction agent for first step extractor, the extraction phase of lower floor enters into next stage extractor, but the extraction phase of most end one-level extractor is after being separated, obtain crude phenols and 1# extraction agent, wherein, 1# extraction agent provides 1# extraction agent for one-level extractor, wherein, m+n=L-1, n=0 ~ L-2, m=1 ~ L-1, the actual amount of the 2# extraction agent of value required for extractor at different levels of m is determined.
When the extracting phase of most end m level extractor, when not reaching the standard of reuse 1# extractor, stop as one-level extractor provides extraction agent, but by this extracting phase after being separated, after extracting 2# extraction agent, again for first step extractor provides extraction agent, m=1 ~ L-1.
Compared with prior art, the present invention at least has the following advantages: the present invention has broken the extracting-back extraction technique that traditional extraction proposes phenol employing, extraction agent of the present invention repeatedly extracts, the content of impurity neutral oil in extraction phase can be reduced, through 3 extractions, phenol relative purity can reach more than 97%, and through 5 extractions, crude phenols relative purity can reach higher.
[accompanying drawing explanation]
Fig. 1 is three grades of extraction process flow skeleton diagrams.
Fig. 2 is five grades extraction technological process block-diagram.
[embodiment]
Following according to Figure of description to a preferred embodiment of the present invention will be described in detail:
The invention provides device and extracting method that phenolic product is put forward in a kind of middle coalite tar extraction, specific as follows:
Extraction process (for three grades of extractions): during nominal situation, the extraction phase in 1# extractor enters the extractor of connecting with 1# extractor successively; Extraction agent in 2# extraction agent storage tank enters other extractors except 1# extractor successively; Extracting phase in most end two extractors of series connection enters 2# extraction agent surge tank, and the extracting phase in all the other extractors enters 2# distiller; Extraction agent in 2# extraction agent surge tank enters 1# extractor; The extraction phase of last extractor of series connection enters 1# distiller.When in GC display 2# extraction agent surge tank output extraction agent, impure amount exceeds standard, the extraction agent in 2# extraction agent surge tank enters 2# distiller, and the extraction agent in 2# extraction agent storage tank enters 1# extractor.
Device annexation (for three grades of extractions): all extractor series connection, 1# extraction agent outlet is connected with 1# extractor entrance, and 2# extraction agent storage tank is connected respectively with other extractor storage tanks that 1# extractor is connected; The extracting phase outlet coming two last extractors in the extractor group of series connection is connected with 2# extraction agent surge tank, and the extracting phase outlet of all the other extractors is connected with 2# distiller; The extraction phase outlet of last extractor of series connection is connected with 1# distiller; When in GC display 2# extraction agent surge tank output extraction agent, impure amount exceeds standard, enable the pipeline that 2# extraction agent outlet is connected with 1# extractor entrance, 2# extraction agent surge tank exports the pipeline be connected with 1# extractor entrance and stops using, and 2# extraction agent outlet and 2# distiller entrance pipe are enabled.
Refer to shown in Fig. 1, for three grades of extractions, coal tar import is connected with 0# distiller, and distill the coal tar obtained and be connected with 1# extractor containing the outlet of phenol fraction section, all the other enter 0# storage tank.The extraction phase outlet of 1# extractor is connected with the import of 2# extractor, the extracting phase outlet of 1# extractor is connected with 2# distiller, the extraction phase outlet of 2# extractor is connected with the import of 3# extractor, the extracting phase outlet of 2# extractor is connected with 2# extraction agent surge tank, the extraction phase outlet of 3# extractor is connected with 1# distiller, the extracting phase outlet of 3# extractor is connected with 2# extraction agent surge tank, the outlet of 1# distiller is connected with 1# extraction agent storage tank, 1# extraction agent outlet is connected with the import of 1# extractor, the outlet of 2# extraction agent surge tank is connected with the import of 1# extractor, 2# extraction agent surge tank alternate outlets is connected with 2# distiller, the outlet of 2# distiller is connected with 2# extraction agent storage tank, obtain dephenolize oil simultaneously, three outlets established by 2# extraction agent storage tank, wherein 2 are connected with the import of 3# extractor with 2# extractor respectively, 3rd is that alternate outlets is connected with 1# extractor, 1#, two imports for subsequent use respectively established respectively by 2# extraction agent storage tank, for adjusting extraction agent proportioning composition.
Refer to shown in Fig. 2, for five grades extraction, extraction process (for five grades extraction): during nominal situation, the extraction phase in 1# extractor enters the extractor of connecting with 1# extractor successively; Extraction agent in 2# extraction agent storage tank enters other extractors except 1# extractor successively; Extracting phase in most end two extractors of series connection enters 2# extraction agent surge tank, and the extracting phase in all the other extractors enters 2# distiller; Extraction agent in 2# extraction agent surge tank enters 1# extractor; The extraction phase of last extractor of series connection enters 1# distiller.When in GC display 2# extraction agent surge tank output extraction agent, impure amount exceeds standard, the extraction agent in 2# extraction agent surge tank enters 2# distiller, and the extraction agent in 2# extraction agent storage tank enters 1# extractor.
Device annexation (for five grades extraction): all extractor series connection, 1# extraction agent outlet is connected with 1# extractor entrance, and 2# extraction agent storage tank is connected respectively with other extractor storage tanks that 1# extractor is connected; The extracting phase outlet coming two last extractors in the extractor group of series connection is connected with 2# extraction agent surge tank, and the extracting phase outlet of all the other extractors is connected with 2# distiller; The extraction phase outlet of last extractor of series connection is connected with 1# distiller; When in GC display 2# extraction agent surge tank output extraction agent, impure amount exceeds standard, enable the spare duct that 2# extraction agent outlet is connected with 1# extractor entrance, 2# extraction agent surge tank exports the pipeline be connected with 1# extractor entrance and stops using, and 2# extraction agent outlet and 2# distiller entrance spare duct are enabled.
Refer to shown in Fig. 2, for five grades extraction, coal tar import is connected with 0# distiller, and distill the coal tar obtained and be connected with 1# extractor containing the outlet of phenol fraction section, all the other enter 0# storage tank.The extraction phase outlet of 1# extractor is connected with the import of 2# extractor, the extracting phase outlet of 1# extractor is connected with 2# distiller, the extraction phase outlet of 2# extractor is connected with the import of 3# extractor, the extracting phase outlet of 2# extractor is connected with 2# distiller, the extraction phase outlet of 3# extractor is connected with the import of 4# extractor, the extracting phase outlet of 3# extractor is connected with 2# distiller, the extraction phase outlet of 4# extractor is connected with the import of 5# extractor, the extracting phase outlet 2# extraction agent surge tank of 4# extractor is connected, the extraction phase outlet of 5# extractor is connected with 1# distiller, the extracting phase outlet of 5# extractor is connected with 2# extraction agent surge tank, the outlet of 1# distiller is connected with 1# extraction agent storage tank, 1# extraction agent outlet is connected with the import of 1# extractor, the outlet of 2# extraction agent surge tank is connected with the import of 1# extractor, 2# extraction agent surge tank alternate outlets is connected with 2# distiller, the outlet of 2# distiller is connected with 2# extraction agent storage tank, obtain dephenolize oil simultaneously, five outlets established by 2# extraction agent storage tank, wherein 4 respectively with 2# extractor, 3# extractor, 4# extractor is connected with the import of 5# extractor, 5th is that alternate outlets is connected with 1# extractor, 1#, two imports for subsequent use respectively established respectively by 2# extraction agent storage tank, for adjusting extraction agent proportioning composition.
The raw material of this art breading comprises coal tar (comprising coal-tar heavy oil, coal-tar middle oil, coalite tar, middle coalite tar), coal tar containing phenol fraction section and other carbolic oil classes.Be particularly useful for middle coalite tar containing phenol fraction section.
For reaching better effects, suggestion at least adopts 3 grades of extraction process (process flow diagram as shown in Figure 1), the extractor of extractor 4,5 (technical process as shown in Figure 2) or more can be set up as required, to improve the phenol purity extracted further.
In addition, in the present invention, the extracting phase of the extractor of most end two-stage is selected to enter into 2# extraction agent surge tank, this is a kind of selection of optimum, in actual use, can enter into 2# extraction agent surge tank according to 1# extractor to the extracting phase that the consumption situation of 2# extraction agent selects the extracting phase of most end one-level extractor to enter into the extractor of 2# extraction agent surge tank or most end three grades or level Four, the extracting phase of remaining other extractor enters in 2# distiller for extracting 2# extraction agent.
In order to realize object of the present invention, described 1# extraction agent storage tank, 2# extraction agent storage tank, and 2# extraction agent surge tank can save not.If 2# extraction agent surge tank does not remove not, so the extractor extracting phase of most end two-stage directly enters into first step extractor, its consumption number can pass through Valve controlling.If it is good that consumption controls, so 1# extraction agent storage tank, 2# extraction agent storage tank, and 2# extraction agent surge tank can all remove, like this, the 1# extraction agent that 1# distiller is separated directly enters into first step extractor, and the 2# extraction agent that 2# distiller is separated directly enters into second to the extractor of most final stage.
During experiment, stirred by middle coalite tar, take 2kg, add RECTIFYING APPARATUS USED IN LABORATORY, regulation system pressure is 0.07MPa, collects <200 DEG C of fraction section, and be coal tar containing phenol fraction section, all the other enter 0# storage tank.
Coal tar enters in 1# extractor containing phenol fraction section, adds the 1# extraction agent in 1# extraction agent storage tank and the 2# extraction agent in 2# extraction agent regulating tank simultaneously, in 1# extractor, carries out extracting operation.Upper phase extracting phase in 1# extractor enters 2# distiller and distills, and the 2# extraction agent steamed enters 2# extraction agent storage tank, and all the other send system for dephenolize oil; Lower phase extraction phase in 1# extractor enters in 2# extractor, carries out second time extracting operation with the 2# extraction agent provided in 2# extraction agent storage tank.Upper phase extracting phase in 2# extractor enters 2# extraction agent regulating tank, and lower phase extraction phase enters 3# extractor, carries out third time extracting operation with the 2# extraction agent provided in 2# extraction agent storage tank.Upper phase extracting phase in 3# extractor enters 2# extraction agent regulating tank, and lower phase extraction phase enters 1# distiller.1# distiller distills the product crude phenols obtained and exports system, and all the other enter 1# extraction agent storage tank.1# extraction agent storage tank exports 1# extraction agent and enters 1# extractor, and 2# extraction agent regulating tank exports 2# extraction agent and enters 1# extractor, so far completes the working cycle of 1 extraction agent.
In view of extraction agent recycles, when long period is run continuously, appearance is fluctuated by 1#, 2# extraction agent liquid in storage tank proportioning, the composition of extraction agent tank output liquid is detected constantly by GC, when liquid proportion exceeds given operating condition scope, entrance for subsequent use can be opened, liquid proportion in adjustment storage tank.When in GC detection display 2# extraction agent regulating tank output extraction agent, impure amount exceeds standard, close the pipeline that 2# extraction agent regulating tank exports to 1# extractor ingress, start pipeline shown in dotted line in figure, liquid in 2# extraction agent regulating tank is made to enter 2# distiller, what distill out is the 2# extraction agent after removal of impurities, be stored in 2# extraction agent storage tank, then enter 1# extractor by the output of 2# extraction agent storage tank, carry out extracting operation.
Compared with prior art, beneficial effect of the present invention is:
1. cut carbolic oil fraction section by distillation, the phenolic component in enrichment coal tar, then carry out extracting operation, can extraction efficiency be improved.
2. adopt composite extractant to carry out extraction and carry phenol, avoid consuming a large amount of soda acid, producing unmanageable phenolic wastewater.
3.2# extraction agent repeatedly extracts, and can reduce the content of impurity neutral oil in extraction phase, and through 3 extractions, phenol relative purity can reach more than 97%, and through 5 extractions, crude phenols relative purity can Da Genggao.
4. this operational path is simple, by adjustment extractor quantity, improves crude phenols quality further, meets higher quality product demand.
5. on 1# extraction agent storage tank, 2# extraction agent storage-tank effluent line, set up GC detect, can according to detected result by reserved import for subsequent use, extraction agent proportioning (as shown in imaginary point line in figure) in adjustment storage tank, to solve the extraction agent component fluctuation problem that may occur in long-term utilization.
6., by completing the extracting phase of extraction process in most end two-stage extractor without Distillation recovery 2# extraction agent, directly carrying out reuse, effectively reducing energy consumption, improve economy.
7. on 2# extraction agent regulating tank outlet line, set up GC detect, if detected result display impurity content exceeding index, then close GC place Trunk Line, start active redundancy pipeline (as shown in phantom in FIG.), the extraction agent of contaminant overstandard is carried out distilation, avoids impact to put forward phenol effect.
Claims (10)
1. the device of phenolic product is carried in coalite tar extraction in one kind, it is characterized in that: comprise extractor and separator, extractor is L and is connected in series, wherein, the extraction phase of upper level extractor enters into next stage extractor, the extraction phase of most end one-level extractor, after 1# separator is separated, obtains crude phenols product and 1# extraction agent, and the 1# extraction agent separated provides extraction agent for first step extractor; The equal direct circulation reuse of extracting phase of most end m extractor provides 2# extraction agent for 1# extractor, the extracting phase of other extractor is after 2# separator is separated, obtain dephenolize oil and 2# extraction agent, wherein, the consumption of the 2# extraction agent of value required for first step extractor of m is determined, m=1 ~ L-1.
2. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 1, it is characterized in that: the 2# extraction agent source line of other extractors except first step extractor is provided with 2# extraction agent adjustment entrance, with supplementary 2# Solvent quantity and the proportioning adjusting 2# extraction agent.
3. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 1, it is characterized in that: the 1# extraction agent source line of described first step extractor is provided with 1# extraction agent adjustment entrance, with supplementary 1# Solvent quantity and the proportioning adjusting 1# extraction agent.
4. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 1, it is characterized in that: the device that phenolic product is put forward in described middle coalite tar extraction includes 2# extraction agent surge tank further, the entrance of this 2# extraction agent surge tank exports with the extracting phase of m extractor of most end and is connected, and the outlet of this 2# extraction agent surge tank is connected with the 2# extraction agent entrance of 1# extractor.
5. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 4, it is characterized in that: the device that phenolic product is put forward in described middle coalite tar extraction comprises 1# extraction agent storage tank and 2# extraction agent storage tank further, the 1# extraction agent that most end one-level extractor is separated is stored in 1# extraction agent storage tank, the extracting phase of other extractors except most end m extractor is after being separated, and the 2# extraction agent obtained is stored in 2# extraction agent storage tank.
6. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 5, it is characterized in that: described 2# extraction agent storage tank is provided with alternate outlets and is connected with the entrance of first step extractor; Described 2# extraction agent surge tank is provided with alternate outlets, and this alternate outlets is connected with the entrance of 2# separator; When the contaminant overstandard of extraction agent in 2# extraction agent surge tank, respective alternate outlets enabled respectively by 2# extraction agent surge tank and 2# extraction agent storage tank.
7. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 1 or 6, it is characterized in that: the device that phenolic product is put forward in described middle coalite tar extraction includes 0# separator further, coal tar is after this 0# separator is separated, the coal tar obtained is connected with first step extractor entrance containing the outlet of phenol fraction section, remainingly enters 0# storage tank mutually.
8. the device of phenolic product is carried in a kind of middle coalite tar extraction according to claim 5, it is characterized in that: the outlet line of 1# extraction agent storage tank and 2# extraction agent storage tank is respectively arranged with extractant concentration proofing unit, according to detected result by reserved mouth for subsequent use, extraction agent proportioning in adjustment storage tank; The outlet line of described 2# extraction agent surge tank is provided with impurity detection device, if detected result display impurity content exceeding index, then close the Trunk Line at proofing unit place, start active redundancy pipeline, comprise 2# extraction agent surge tank to the active redundancy pipeline of 2# separator and 2# extraction agent storage tank to the active redundancy pipeline of 1# extractor.
9. in, a method for phenolic product is put forward in coalite tar extraction, it is characterized in that: this device putting forward phenolic product comprises L extractor and 1# and 2# extraction agent separator, wherein, is connected in series between L extractor; Specifically comprise the following steps:
(1) after 1#, 2# two kinds of extraction agents and coal tar fraction section carry out extraction process in first step extractor, the extraction phase of lower floor enters into the extractor of next stage, and the extracting phase on upper strata, after 2# separator is separated, obtains 2# extraction agent and dephenolize oil;
(2) extract successively under the effect of the extraction phase that provides at upper level extractor successively of second stage extractor and n extractor being connected in series with it and 2# extraction agent, after having extracted, the extracting phase on upper strata is separated through 2# separator, obtain 2# extraction agent and dephenolize oil, the extraction phase of lower floor enters into next stage extractor;
(3) extract successively under the effect of the extraction phase that m the extractor being positioned at most end provides at upper level extractor and 2# extraction agent, after having extracted, the extracting phase on upper strata provides 2# extraction agent for first step extractor, the extraction phase of lower floor enters into next stage extractor, the most finally the last grade of extractor extraction process enters 1# separator after completing, after being separated, obtain crude phenols and 1# extraction agent, wherein, 1# extraction agent provides 1# extraction agent for one-level extractor, wherein, m+n=L-1, n=0 ~ L-2, m=1 ~ L-1, the value of m is determined by the actual amount of extractor 2# extraction agent at different levels.
10. the method for phenolic product is put forward in a kind of middle coalite tar extraction according to claim 9, it is characterized in that: when the extracting phase of most end m level extractor, when not reaching the standard of reuse 1# extractor, stop providing extraction agent for one-level extractor, but by this extracting phase after being separated, after extracting 2# extraction agent, again for first step extractor provides extraction agent, m=1 ~ L-1.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105802651A (en) * | 2016-04-26 | 2016-07-27 | 榆林学院 | Method for extracting phenolic compound in low-temperature coal tar by using ionic liquid |
| CN106566571A (en) * | 2016-11-07 | 2017-04-19 | 山东科技大学 | Coal tar complexation method dephenolization device |
| CN106867556A (en) * | 2017-03-01 | 2017-06-20 | 西北大学 | A kind of coal tar fraction separating technology and device |
| CN115253378A (en) * | 2022-07-27 | 2022-11-01 | 郑州天一萃取科技有限公司 | Multistage centrifugal extraction system and centrifugal extractor for multistage extraction |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010100518A1 (en) * | 2009-03-03 | 2010-09-10 | Litwin | Process for the treatment of phenol and tar acids containing oil |
| CN102465033A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Processing method of medium-low temperature coal tar |
| CN102585870A (en) * | 2012-02-15 | 2012-07-18 | 中国矿业大学 | Method for quickly separating chain hydrocarbon and phenols from medium and low temperature tar |
| CN103215058A (en) * | 2013-05-02 | 2013-07-24 | 枣庄矿业集团煤化工研究院有限公司 | Method for extracting and separating light component from coal tar at low temperature |
| CN203139681U (en) * | 2013-02-07 | 2013-08-21 | 陕西煤业化工技术研究院有限责任公司 | Complete equipment for separating and extracting phenols in middle-temperature and low-temperature coal tar by extraction method |
| CN203683420U (en) * | 2013-09-06 | 2014-07-02 | 山西省国新能源发展集团有限公司 | Novel device for quickly separating phenol compounds in coal tar |
| CN205024164U (en) * | 2015-09-16 | 2016-02-10 | 陕西煤业化工技术研究院有限责任公司 | Device of phenolic constituents result is carried in extraction of well low temperature coal tar |
-
2015
- 2015-09-16 CN CN201510589737.6A patent/CN105112084A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010100518A1 (en) * | 2009-03-03 | 2010-09-10 | Litwin | Process for the treatment of phenol and tar acids containing oil |
| CN102465033A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Processing method of medium-low temperature coal tar |
| CN102585870A (en) * | 2012-02-15 | 2012-07-18 | 中国矿业大学 | Method for quickly separating chain hydrocarbon and phenols from medium and low temperature tar |
| CN203139681U (en) * | 2013-02-07 | 2013-08-21 | 陕西煤业化工技术研究院有限责任公司 | Complete equipment for separating and extracting phenols in middle-temperature and low-temperature coal tar by extraction method |
| CN103215058A (en) * | 2013-05-02 | 2013-07-24 | 枣庄矿业集团煤化工研究院有限公司 | Method for extracting and separating light component from coal tar at low temperature |
| CN203683420U (en) * | 2013-09-06 | 2014-07-02 | 山西省国新能源发展集团有限公司 | Novel device for quickly separating phenol compounds in coal tar |
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