CN102512961A - Technology for purifying wood vinegar - Google Patents
Technology for purifying wood vinegar Download PDFInfo
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- CN102512961A CN102512961A CN2011103331290A CN201110333129A CN102512961A CN 102512961 A CN102512961 A CN 102512961A CN 2011103331290 A CN2011103331290 A CN 2011103331290A CN 201110333129 A CN201110333129 A CN 201110333129A CN 102512961 A CN102512961 A CN 102512961A
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- pyroligneous acid
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- wood vinegar
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Abstract
The invention relates to a technology for purifying wood vinegar, which comprises a pretreatment part and a membrane separation part, and comprises the steps of: leading wood vinegar stock solution to firstly enter into a stock solution box, pretreating, filtering particle impurities which are larger than 1mu m, and then leading the filtered wood vinegar stock solution into the membrane separation part; inputting the pretreated wood vinegar stock solution into an ultrafiltration device, returning the concentrated liquid into the stock solution box after ultrafiltration, and conveying the dilute liquid into a first stage filtrate box; carrying out nanofiltration, conveying the separated concentrated liquid into a purified wood vinegar liquid box, and conveying the separated dilute liquid into a second stage filtrate box; carrying out high-pressure reverse osmosis, conveying the separated concentrated liquid into the purified wood vinegar liquid box, and conveying the separated dilute liquid into a third stage filtrate box; and finally, carrying out low-pressure reverse osmosis, conveying the separated concentrated liquid into the purified wood vinegar liquid box, and conveying the separated dilute liquid into a fresh water box. When being used for purifying the wood vinegar, the technology is high in production efficiency, the extracted wood vinegar is high in purity, and the energy consumption is low; and the application of the technology is beneficial to promoting the comprehensive utilization of biomass such as straw and the like.
Description
Technical field
Invention relates to a kind of technology of utilizing membrane separation technique to carry out the pyroligneous acid purifying.
Background technology
Pyroligneous acid is to utilize stalk and other agriculture and forestry organic waste material to carry out a kind of product of charing, gasification production process output, and it contains more than 200 kind of organic matter, has important use aspect desinsection, sterilization, promotion plant growth and food fresh keeping, the beauty and health care.But the pyroligneous acid stoste of production process output contains a large amount of moisture and impurity, and content of organics only has about 6%, influences effective utilization of pyroligneous acid, causes a large amount of pyroligneous acids of output to go out of use, and has both caused the wasting of resources, causes secondary pollution again.At present, the purifying of pyroligneous acid is also done big quantity research both at home and abroad, mainly contained settled process, the way of distillation, filtration method, apportion design, absorption method, electrostatic method, freezing etc.; But these technical methods; The power consumption that has is high, and the treatment effeciency that has is low, and the purification degrees that has is very low, water content is big.Therefore, the purifying of pyroligneous acid is still a technical barrier so far, has influenced the comprehensive development and utilization with living beings such as stalks of applying of pyroligneous acid.
Summary of the invention
The purpose of this invention is to provide a kind of pyroligneous acid purifying process, transform the product of simmer down to higher degree to pyroligneous acid stoste, overcoming the deficiency that prior art exists, apply the creation technical conditions for pyroligneous acid.
Pyroligneous acid purifying process of the present invention; Comprise preprocessing part and film separating part; Pyroligneous acid stoste is introduced into the stoste case, sends into mechanical filter 1, mechanical filter 2 by compression pump 1, gets into smart filter 1, smart filter 2 filterings again and gets into the film separating part after greater than 1 μ m granule foreign; With pretreated pyroligneous acid stoste input ultrafiltration apparatus, when the dope flow that is back to the stoste case through flowmeter 1 reached the 50%-70% of ultrafiltration total flow, the light liquid through flowmeter 2 was conveyed into the one-level filtrate box; The liquid level of one-level filtrate box reaches at 50% o'clock and refluxes through choke valve, regulates flow and pressure, and starting pressure pump 2 gets into nanofiltration, and isolated dope is conveyed into pyroligneous acid refined solution case, and light liquid is conveyed into the secondary filtrate box; Secondary filtrate box liquid level reaches at 50% o'clock, refluxes through choke valve, regulates flow and pressure, and starting pressure pump 3 gets into the high pressure counter-infiltration, and isolated dope is conveyed into pyroligneous acid refined solution case, and light liquid is conveyed into three grades of filtrate box; Reflux through choke valve, regulate flow and pressure, get into low pressure reverse osmosis, isolated dope is conveyed into pyroligneous acid refined solution case, and isolated light liquid is conveyed into fresh-water tank; The pyroligneous acid of pyroligneous acid refined solution case is got product after by the standard can; To entering the water of fresh-water tank,, detection can discharge or recycle after reaching discharge standard, do not reach the after-treatment of carrying out of discharge standard.
Preprocessing part is made up of stoste case, compression pump 1, mechanical filter 1, mechanical filter 2 and smart filter 1, smart filter 2, and each device is connected with pipeline; The filtering material of mechanical filter 1, mechanical filter 2 is quartz sand or filtering materials such as active carbon or adsorptive resin; The filter core of essence filter 1, smart filter 2 is polypropylene filter core or ceramic element, or the ability filtering is greater than other filter core of 1 μ m granule foreign;
The film separating part mainly is made up of device such as ultrafiltration, one-level filtrate box, compression pump 2, nanofiltration, secondary filtrate box, compression pump 3, high pressure counter-infiltration, three grades of filtrate box, compression pump 4, low pressure reverse osmosis and servicing unit, and each device is connected with pipeline; The ultrafiltration apparatus core parts are hollow fiber ultrafiltration membrane, are called for short UF, and inlet links to each other with the essence filter 2 of preprocessing part with pipeline; The dope outlet is connected with the stoste case with choke valve 1, flowmeter 1 with pipeline, can not pass back into the stoste case through the dope of filter membrane, strengthens the flow and the flow velocity on milipore filter surface simultaneously through refluxing; Light liquid outlet is connected with the one-level filtrate box with choke valve 2, flowmeter 2 with pipeline, with light liquid input one-level filtrate box, supplies the next stage separating treatment; The core parts of nanofiltration device are NF membrane, are called for short NF, and its inlet links to each other with compression pump 3, one-level filtrate box with pipeline; The dope outlet links to each other with pyroligneous acid refined solution case with choke valve 5, flowmeter 4 with pipeline; Light liquid outlet links to each other with the secondary filtrate box with choke valve 4, flowmeter 3 with pipeline, and light liquid input secondary filtrate box is supplied subordinate's separating treatment; The two ends liquid import and export of compression pump 2 is with pipeline and choke valve 3 composition return flow lines, in order to regulate the operating pressure of NF membrane; The core parts of high pressure reverse osmosis unit are that reverse osmosis membrane is called for short RO; Its inlet links to each other with the secondary filtrate box with compression pump 3 through pipeline; The dope outlet links to each other with pyroligneous acid refined solution case with choke valve 8, flowmeter 6 with pipeline; Light liquid outlet links to each other with three grades of filtrate box with choke valve 7, flowmeter 5 with pipeline, with three grades of filtrate box of light liquid input, supplies the next stage separating treatment; The two ends liquid import and export of compression pump 3 is with pipeline and choke valve 6 composition return flow lines, in order to regulate the operating pressure of high pressure counter-infiltration; The core parts of low pressure reverse osmosis device are all reverse osmosis membrane and are called for short RO, but its operating pressure is lower, and its inlet links to each other with three grades of filtrate box with compression pump 4 through pipeline; The dope outlet links to each other with pyroligneous acid refined solution case with choke valve 11, flowmeter 8 with pipeline; Water outlet links to each other with fresh-water tank with choke valve 10, flowmeter 7 with pipeline; The two ends liquid import and export of compression pump 4 is with pipeline and choke valve 9 composition return flow lines, in order to regulate the operating pressure of low pressure reverse osmosis.
Preprocessing part of the present invention mainly is falling greater than larger particles Impurity removals such as the suspended material of 1 μ m and flocculent substances, guaranteeing carrying out smoothly of subsequent film processing.
Good effect of the present invention is: through technology of the present invention pyroligneous acid stoste is concentrated purification and be the higher refined solution of content of organics; Make it become a kind of valuable biochemical industry raw material; Turn waste into wealth; Reduce pollutant emission biomass carbonated, the gasification production process, help promoting the comprehensive utilization of living beings such as stalk; Pyroligneous acid purifying process production efficiency of the present invention is high, power consumption is low, helps saving energy and reduce the cost.
Description of drawings
Accompanying drawing is a pyroligneous acid purifying process schematic flow sheet.
The specific embodiment
(1) preparatory stage: with the pyroligneous acid stoste pyroligneous acid stoste case of packing into, close choke valve 2, open choke valve 1; (2) the starting pressure pump 1, and the pressurization of pyroligneous acid stoste is given processing through mechanical filter 1, mechanical filter 2 and smart filter 1, smart filter 2 successively, removes the above granule foreign of 5 μ m in the stoste, and will give the stoste input ultrafiltration apparatus after the processing; (3) open choke valve 2; And turn choke valve 1 down, and flowmeter 1, flowmeter 2 are observed in the limit, and choke valve 1, choke valve 2 are regulated in the limit; The 50%-70% that makes the dope flow that is back to the stoste case through flowmeter 1 reach the ultrafiltration total flow gets final product, and the light liquid through flowmeter 2 is conveyed into the one-level filtrate box; (4) running of nanofiltration device: close choke valve 4, choke valve 5 earlier, open choke valve 3, the liquid level of one-level filtrate box reaches at 50% o'clock and starts force (forcing) pump 2; After treating that compression pump 2 starts normally; Open choke valve 4 earlier, slowly open choke valve 5 simultaneously and regulate backflow choke valve 3, through regulating choke valve 3; Make the operating pressure of nanofiltration device reach the pressure parameter that requires formulation according to purification degrees; Flowmeter 3, flowmeter 4 are observed in the limit then, and choke valve 4, choke valve 5 are regulated in the limit, make the flow-rate ratio through flowmeter 3, flowmeter 4 meet the parameter that requires formulation according to purification degrees; Isolated dope is conveyed into pyroligneous acid refined solution case, and light liquid is conveyed into the secondary filtrate box; (5) running of high pressure reverse osmosis unit; At first open choke valve 6, close choke valve 7, choke valve 8, secondary filtrate box liquid level reaches 50% o'clock starting pressure pump 3; After treating that compression pump 3 works well; Open choke valve 7 earlier, open choke valve 8 more simultaneously and regulate choke valve 6, make the operating pressure of reverse osmosis unit reach the pressure parameter that requires formulation according to purification degrees through regulating choke valve 6; Flowmeter 5, flowmeter 6 are observed in the limit then; Limit adjustment choke valve 7, shutoff valve 8 make dope and the light flow quantity ratio through flowmeter 5 through flowmeter 6, meet according to purification degrees to require the parameter confirmed; Isolated dope output pyroligneous acid refined solution case, light liquid is conveyed into three grades of filtrate box; (6) the operation principle of low pressure reverse osmosis device is identical with the high pressure counter-infiltration; But its running is worked under lower pressure; The pressure adjustment should meet the parameter of confirming according to production requirement, isolated dope input pyroligneous acid refined solution case, isolated fresh water input fresh-water tank; (7) pyroligneous acid of pyroligneous acid refined solution case is got product after by the standard can; (8) to entering the fresh water of fresh-water tank, after detection reaches discharge standard, both can discharge or recycle, should not carry out after-treatment when reaching discharge standard.
The operation principle of film processing section is such: milipore filter is used for molecular cut off greater than 500 material, mainly is to come out the dissolubility tar separation; Use the organic substance of NF membrane molecular cut off as 200-500, the relatively large pyroligneous acid composition of a part of molecular weight from coming out; Adopt reverse osmosis membrane to separate the pyroligneous acid composition of the overwhelming majority at last, and exclude the contained moisture of pyroligneous acid stoste.Counter-infiltration adopts high-pressure osmosis and low-pressure permeability to combine; The high pressure counter-infiltration is the organic matter of under higher operating pressure, holding back greater than hydrone; Low pressure reverse osmosis is the organic matter of under lower pressure, further holding back greater than hydrone, and the pyroligneous acid composition and the moisture of the overwhelming majority are left.Organic matter under nanofiltration, high pressure counter-infiltration, low pressure reverse osmosis are held back is the pyroligneous acid refined solution, and from the liquid that the outlet of the light liquid of low pressure reverse osmosis device is discharged be can qualified discharge fresh water.
Claims (1)
1. pyroligneous acid purifying process; Comprise preprocessing part and film separating part; Pyroligneous acid stoste is introduced into the stoste case, sends into mechanical filter 1, mechanical filter 2 by compression pump 1, gets into smart filter 1, smart filter 2 filterings again and gets into the film separating part after greater than 1 μ m granule foreign; With pretreated pyroligneous acid stoste input ultrafiltration apparatus, when the dope flow that is back to the stoste case through flowmeter 1 reached the 50%-70% of ultrafiltration total flow, the light liquid through flowmeter 2 was conveyed into the one-level filtrate box; The liquid level of one-level filtrate box reaches at 50% o'clock and refluxes through choke valve, regulates flow and pressure, and starting pressure pump 2 gets into nanofiltration, and isolated dope is conveyed into pyroligneous acid refined solution case, and light liquid is conveyed into the secondary filtrate box; Secondary filtrate box liquid level reaches at 50% o'clock, refluxes through choke valve, regulates flow and pressure, and starting pressure pump 3 gets into the high pressure counter-infiltration, and isolated dope is conveyed into pyroligneous acid refined solution case, and light liquid is conveyed into three grades of filtrate box; Reflux through choke valve, regulate flow and pressure, get into low pressure reverse osmosis, isolated dope is conveyed into pyroligneous acid refined solution case, and isolated light liquid is conveyed into fresh-water tank; The pyroligneous acid of pyroligneous acid refined solution case is got product after by the standard can; To entering the water of fresh-water tank,, detection can discharge or recycle after reaching discharge standard, do not reach the after-treatment of carrying out of discharge standard.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103331290A CN102512961A (en) | 2011-10-28 | 2011-10-28 | Technology for purifying wood vinegar |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103331290A CN102512961A (en) | 2011-10-28 | 2011-10-28 | Technology for purifying wood vinegar |
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| CN102512961A true CN102512961A (en) | 2012-06-27 |
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| CN2011103331290A Pending CN102512961A (en) | 2011-10-28 | 2011-10-28 | Technology for purifying wood vinegar |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560090A (en) * | 2014-12-30 | 2015-04-29 | 蓝星环境工程有限公司 | Integrated process for refining and separating crude wood vinegar |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0649454A (en) * | 1992-07-27 | 1994-02-22 | Katsunori Karasawa | Purification of pyrolignous acid |
| JP2005255865A (en) * | 2004-03-12 | 2005-09-22 | Odaka Ringyo:Kk | Method for producing highly purified pyroligneous acid |
| CN101368106A (en) * | 2008-09-12 | 2009-02-18 | 河南省化工研究所有限责任公司 | Purifying process for solution of wood vinegar |
| CN201823331U (en) * | 2010-09-14 | 2011-05-11 | 辽宁大学 | Solar rectification and purification device dedicated for crude pyroligneous acid |
-
2011
- 2011-10-28 CN CN2011103331290A patent/CN102512961A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0649454A (en) * | 1992-07-27 | 1994-02-22 | Katsunori Karasawa | Purification of pyrolignous acid |
| JP2005255865A (en) * | 2004-03-12 | 2005-09-22 | Odaka Ringyo:Kk | Method for producing highly purified pyroligneous acid |
| CN101368106A (en) * | 2008-09-12 | 2009-02-18 | 河南省化工研究所有限责任公司 | Purifying process for solution of wood vinegar |
| CN201823331U (en) * | 2010-09-14 | 2011-05-11 | 辽宁大学 | Solar rectification and purification device dedicated for crude pyroligneous acid |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104560090A (en) * | 2014-12-30 | 2015-04-29 | 蓝星环境工程有限公司 | Integrated process for refining and separating crude wood vinegar |
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Application publication date: 20120627 |