CN102627618A - Method for producing furfural through biomass hydrolysis-reactive extraction - Google Patents
Method for producing furfural through biomass hydrolysis-reactive extraction Download PDFInfo
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Abstract
本发明公开了一种生物质水解—反应萃取生产糠醛的方法，属于糠醛的生产技术领域。该方法过程包括生物质原料在甲酸和乙酸催化下水解为戊糖溶液；戊糖溶液经过反应萃取工艺制备糠醛，生成的糠醛进入萃取剂中，以萃取相从反应萃取塔底采出；未反应的部分戊糖含酸溶液以萃余相的形式从反应萃取塔顶采出；萃取相进入萃取剂再生塔中，萃取剂再生塔采取减压操作，塔顶采出粗糠醛，塔底的萃取剂送入萃取剂储槽中循环使用；本发明实现了废水零排放，提高了糠醛收率，降低了能耗，扩大了糠醛生产的原料范围，水解后生物质中的纤维素和木质素几乎未被破坏，实现原料的综合利用。The invention discloses a biomass hydrolysis-reaction extraction method for producing furfural, which belongs to the technical field of furfural production. The process of the method includes the hydrolysis of biomass raw materials into a pentose solution under the catalysis of formic acid and acetic acid; the pentose solution undergoes a reaction extraction process to prepare furfural, and the generated furfural enters the extraction agent, and is extracted from the bottom of the reaction extraction tower as an extraction phase; unreacted Part of the pentose acid-containing solution is extracted from the top of the reaction extraction tower in the form of a raffinate phase; the extraction phase enters the extraction agent regeneration tower, and the extraction agent regeneration tower adopts a decompression operation, the crude furfural is extracted from the top of the tower, and the extraction at the bottom of the tower The extraction agent is sent to the extractant storage tank for recycling; the invention realizes zero discharge of waste water, improves the yield of furfural, reduces energy consumption, expands the range of raw materials for furfural production, and almost no cellulose and lignin in the biomass after hydrolysis be destroyed to realize the comprehensive utilization of raw materials.
Description
Technical field
The present invention relates to a kind of biomass by hydrolyzation-reaction, extraction and produce the method for furfural, belong to the production technical field of furfural.
Background technology
Furfural has another name called furtural.There are functional groups such as aldehyde radical, diene, cyclic ethers in the furfural molecular structure; So it has the character of aldehyde, ether, diene and arene compound concurrently; Can participate in the reaction of number of different types; Synthetic a lot of Chemicals are widely used in a plurality of production fields such as food, medicine, synthetic resins, casting.
The raw material of producing furfural at present is to be rich in the vegetable fibre of piperylene, like corn cob, bagasse, cornstalk, paddy rice stalk etc.Its principle is that piperylene at first is hydrolyzed to pentose, and the pentose cyclodehydration generates furfural then.
Whether in same reactor drum, can furfural production be divided into single stage method and two-step approach according to this two-step reaction of pentosan hydralysis and pentose dehydration.The single stage method advantage is that equipment is simple, simple to operate, production cost is low, but that its main drawback is a steam consumption is big,, produce the steam that 1 ton of furfural consumes 18～24 tons; Furaldehyde yield is low, has only about 45%; Produce the great amount of wastewater waste residue, produce 1 ton of furfural and produce 24 tons of high pollution waste water; Raw material availability is low, produces 1 ton of furfural, consumes 11 tons of corn cobs; The waste residue blackout, Mierocrystalline cellulose and xylogen destroy serious.Two-step approach is because pentosan hydralysis and pentose dehydration are carried out in two reactor drums, and the raw material availability that has solved existing furfural production is low, furaldehyde yield is low, spent process water is hard to manage, furfural dregs is difficult to continue difficult problems such as utilization.
Summary of the invention
The object of the present invention is to provide a kind of biomass by hydrolyzation-reaction, extraction to produce the method for furfural, this method has advantages such as the raw material comprehensive utilization ratio is high, furaldehyde yield is high, spent process water is few.
The present invention realizes through following technical proposals, and a kind of biomass by hydrolyzation-reaction, extraction is produced the method for furfural, and this method comprises that through employing hydrolysis kettle, reaction, extraction tower, extractant regeneration tower, acid recovery rectifying tower device realize; Its characteristic comprises following process: is 3 ~ 15% the aqueous solution with biomass material with the first and second sour mass concentrations that contain that come from the acid solution storage tank or come from the reaction, extraction tower; Joining in the hydrolysis kettle by mass ratio 1:5 ~ 25, is under 100 ~ 180 ℃ in temperature, hydrolysis 40 ~ 150min; Obtain the pentose mass concentration and be 2 ~ 10% hydrolyzed solution; Hydrolyzed solution and extraction agent Ortho Nitro Toluene are 1:2 ~ 10 by volume, and top and the lower bottom part by the reaction, extraction tower gets into the reaction, extraction tower respectively, is to carry out reaction, extraction under 150 ~ 240 ℃ of conditions in temperature; The extraction phase that is rich in furfural by the bottom extraction of reaction, extraction tower gets into the extractant regeneration tower; This extractant regeneration tower is 0.01MPa at tower top pressure, by the top extraction chaff aldehyde of extractant regeneration tower, again through follow-up refining; Obtain the finished product furfural, get into the reaction, extraction tower by the bottom output extraction agent of extractant regeneration tower and recycle; Enter into the acid recovery tower by the acidiferous extracting phase of reaction, extraction top of tower extraction, acidity is laggard goes into hydrolysis kettle and recycles through reducing.
Biomass described in the said process comprise: wherein one or both of corn cob, wheat stalk, rice straw, cornstalk, sorghum stalk; The first and second sour mass ratioes are 1:3.
Advantage of the present invention has: 1) the first step adopts the sour extracting phase that contains of second step reaction, extraction column overhead extraction to come the hydrolyzing biomass raw material, because acid-bearing wastewater mainly contains acetate and formic acid, the both is an organic acid; Acid with a little less than furfurol industry conventional catalysts sulfuric acid is compared acidity; Low to equipment corrosion, and Mierocrystalline cellulose and xylogen are destroyed hardly in the biomass after the hydrolysis, can continue to utilize; 2) realize containing recycling of aqueous acid, reduced even can avoid the discharging of waste water; 3) the second step pentose dehydration generates furfural and adopts reaction, extraction technology, and the furfural that reaction is generated in time gets in the extraction agent, and then reduces even avoided the side reaction of furfural at aqueous phase, and the yield furaldehyde yield of the present invention that has improved furfural is more than 70%; 4) realize the comprehensive utilization of energy, reduced energy consumption.Major cause is to carry out heat exchange from the acid solution of the extracting phase of reaction, extraction column overhead extraction and entering hydrolysis kettle, reclaims heat; The extraction phase of extraction carries out heat exchange with the extraction agent that enters into the reaction, extraction tower at the bottom of the reaction, extraction Tata, reclaims heat.Along with the development of furfurol industry, and the raising of raw material requirements of comprehensive utilization, the two-step approach furfural production technology will become the inevitable development trend of furfurol industry.
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Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Shown in the figure, 1-acid solution storage tank, 2-hydrolysis kettle, 3-reaction, extraction tower, 4-extraction agent interchanger; 5-extraction agent storage tank, 6-extractant regeneration tower, 7-chaff aldehyde storage tank, 8-reaction, extraction tower phase separation tank, 9-acid recovery reaction fractionating tower, the thick ester storage tank of 10-, the 11-first and second acid recovery tower phase separation tank, 12-pentose solution interchanger.
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Embodiment
Embodiment one
The dry corn cob 40g that crushes is joined in the hydrolysis kettle; Add then quality 400g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 150 ℃, behind the hydrolysis 1h; Filtration obtains the solution 360ml that pentose content is 2.73wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 2:1 gets into the 720ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 180 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).Its total acid value of the surplus mensuration of the collection of cat head extraction is 9.5wt %, does not surpass 15wt %, directly gets in the acid storage tank to recycle.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction enters into the extraction agent storage tank and recycles at the bottom of the tower.Furaldehyde yield is 72%, and the hydrolysis of hemicellulose rate is 95.8%.
Embodiment two
The dry corn cob 60g that crushes is joined in the hydrolysis kettle; Add then quality 300g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 140 ℃, behind the hydrolysis 1h; Filtration obtains the solution 240ml that pentose content is 5wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 3:1 gets into the 720ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 190 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).Its total acid value of the surplus mensuration of the collection of cat head extraction is 8.5wt %, does not surpass 15wt %, directly gets in the acid storage tank to recycle.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction enters into the extraction agent storage tank and recycles filter residue and treat later use at the bottom of the tower.Furaldehyde yield is 66%, and the hydrolysis of hemicellulose rate is 92.5%.
Embodiment three
The dry cornstalk 20g that crushes is joined in the hydrolysis kettle; Add then quality 400g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 160 ℃, behind the hydrolysis 40min; Filtration obtains the solution 380ml that pentose content is 1.52wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 3:1 gets into the 1140ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 200 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).It is 18 wt % that extraction phase is measured its total acid value, surpasses 15wt %, and this acid solution is sent in the acid recovery tower, recycles after the reduction acidity.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction gets in the extraction agent storage tank and recycles at the bottom of the tower.Furaldehyde yield is 69%, and the hydrolysis of hemicellulose rate is 93.3%.
Embodiment four
The wheat stalk 40g that crushes is joined in the hydrolysis kettle; Add then quality 600g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 160 ℃, behind the hydrolysis 60min; Filtration obtains the solution 560ml that pentose content is 1.60wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 3:1 gets into the 1680ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 200 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).It is 18 wt % that extraction phase is measured its total acid value, surpasses 15wt %, and this acid solution is sent in the acid recovery tower, recycles after the reduction acidity.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction gets in the extraction agent storage tank and recycles at the bottom of the tower.Furaldehyde yield is 68%, and the hydrolysis of hemicellulose rate is 96.2%.
Embodiment five
The rice straw 40g that crushes is joined in the hydrolysis kettle; Add then quality 600g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 170 ℃, behind the hydrolysis 60min; Filtration obtains the solution 570ml that pentose content is 1.29wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 2:1 gets into the 1140ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 200 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).It is 18 wt % that extraction phase is measured its total acid value, surpasses 15wt %, and this acid solution is sent in the acid recovery tower, recycles after the reduction acidity.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction gets in the extraction agent storage tank and recycles at the bottom of the tower.Furaldehyde yield is 71%, and the hydrolysis of hemicellulose rate is 95.0%.
Embodiment six
The sorghum stalk 40g that crushes is joined in the hydrolysis kettle; Add then quality 600g from the extraction of reaction, extraction column overhead contain acid hydrolysis liquid in hydrolyzer, keeping the temperature of hydrolysis kettle is 180 ℃, behind the hydrolysis 40min; Filtration obtains the solution 550ml that pentose content is 1.56wt%; Getting at the bottom of the reaction, extraction Tata the tower, is that the ratio of 3:1 gets into the 1650ml extraction agent the tower from the reaction, extraction column overhead in extraction agent and pentose solution volume ratio simultaneously, keeps 200 ℃ of the interior temperature of reaction, extraction tower; The extraction phase of extraction is sent in the extractant regeneration tower at the bottom of the tower, and the extractant regeneration pressure tower is 0.01MPa (A).It is 18 wt % that extraction phase is measured its total acid value, surpasses 15wt %, and this acid solution is sent in the acid recovery tower, recycles after the reduction acidity.The chaff aldehyde of extractant regeneration cat head extraction gets in the thick aldehyde storage tank, and the extraction agent of extraction gets in the extraction agent storage tank and recycles at the bottom of the tower.Furaldehyde yield is 70%, and the hydrolysis of hemicellulose rate is 96.8%.
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104387346A (en) * | 2014-12-01 | 2015-03-04 | 天津大学 | Method for extracting furfural by means of multi-stage continuous countercurrent reaction of pentose |
| CN104557811A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from pentose solution by adopting ultrasonic reactor |
| CN104557806A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Preparation method of 5-hydroxymethylfurfural |
| CN104557812A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from biomass |
| CN104557809A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from pentose |
| CN104557810A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfuraldehyde from pentose solution by adopting impinging stream reactor |
| CN105315243A (en) * | 2015-09-16 | 2016-02-10 | 安庆市宜秀区永兴农机农艺综合发展专业合作社 | Method for preparing furfural through agricultural waste |
| CN106146440A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of production method of furfural |
| CN106146438A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of production technology of furfural |
| CN106146441A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of preparation technology of furfural |
| CN106146439A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of preparation method of furfural |
| CN110105313A (en) * | 2019-04-18 | 2019-08-09 | 肖兵 | A kind of Two-way Cycle furfural production system and technique |
| CN110563675A (en) * | 2019-08-01 | 2019-12-13 | 四川金象赛瑞化工股份有限公司 | Method for preparing furfural by extracting xylose through steam explosion of cotton stalks and full utilization |
| CN113999192A (en) * | 2021-11-19 | 2022-02-01 | 安徽金轩科技有限公司 | Method for extracting furfural from pentose produced by furfural |
| CN116855644A (en) * | 2023-07-19 | 2023-10-10 | 河南禾力能源有限公司 | Process for producing pentose liquid for preparing furfural by using agricultural and forestry biomass combined raw materials |
-
2012
- 2012-03-22 CN CN2012100781026A patent/CN102627618A/en active Pending
Non-Patent Citations (1)
| Title |
|---|
| 李志松等: "玉米芯制备糠醛的研究", 《精细化工中间体》 * |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104557811A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from pentose solution by adopting ultrasonic reactor |
| CN104557806A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Preparation method of 5-hydroxymethylfurfural |
| CN104557812A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from biomass |
| CN104557809A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfural from pentose |
| CN104557810A (en) * | 2013-10-24 | 2015-04-29 | 中国石油化工股份有限公司 | Method for producing furfuraldehyde from pentose solution by adopting impinging stream reactor |
| CN104387346B (en) * | 2014-12-01 | 2016-05-11 | 天津大学 | Prepared the method for furfural by pentose multiple stage continuous adverse current reaction, extraction |
| CN104387346A (en) * | 2014-12-01 | 2015-03-04 | 天津大学 | Method for extracting furfural by means of multi-stage continuous countercurrent reaction of pentose |
| CN106146440A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of production method of furfural |
| CN106146438A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of production technology of furfural |
| CN106146441A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of preparation technology of furfural |
| CN106146439A (en) * | 2015-04-19 | 2016-11-23 | 中国石油化工股份有限公司 | A kind of preparation method of furfural |
| CN105315243A (en) * | 2015-09-16 | 2016-02-10 | 安庆市宜秀区永兴农机农艺综合发展专业合作社 | Method for preparing furfural through agricultural waste |
| CN110105313A (en) * | 2019-04-18 | 2019-08-09 | 肖兵 | A kind of Two-way Cycle furfural production system and technique |
| CN110563675A (en) * | 2019-08-01 | 2019-12-13 | 四川金象赛瑞化工股份有限公司 | Method for preparing furfural by extracting xylose through steam explosion of cotton stalks and full utilization |
| CN110563675B (en) * | 2019-08-01 | 2023-05-30 | 四川金象赛瑞化工股份有限公司 | Method for preparing furfural and fully utilizing xylose by cotton stalk steam explosion extraction |
| CN113999192A (en) * | 2021-11-19 | 2022-02-01 | 安徽金轩科技有限公司 | Method for extracting furfural from pentose produced by furfural |
| CN113999192B (en) * | 2021-11-19 | 2024-01-12 | 安徽金轩科技有限公司 | A method for extracting furfural from pentose sugar |
| CN116855644A (en) * | 2023-07-19 | 2023-10-10 | 河南禾力能源有限公司 | Process for producing pentose liquid for preparing furfural by using agricultural and forestry biomass combined raw materials |
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Application publication date: 20120808 |