CN201428085Y - Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia - Google Patents
Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia Download PDFInfo
- Publication number
- CN201428085Y CN201428085Y CN2009200977410U CN200920097741U CN201428085Y CN 201428085 Y CN201428085 Y CN 201428085Y CN 2009200977410 U CN2009200977410 U CN 2009200977410U CN 200920097741 U CN200920097741 U CN 200920097741U CN 201428085 Y CN201428085 Y CN 201428085Y
- Authority
- CN
- China
- Prior art keywords
- ammonia
- ammoniacal liquor
- retort
- straw
- explosion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The utility model relates to a device for performing crystallization removing to plant straw through adopting the circulating explosion method of gradient fluidized sulfate. The device comprises a straw pulverizer, an ammonia bottle, a plunger pump, an ammonia liquid explosion reaction tank, an ammonia liquid buffer tank, a material reception tank, a solid-liquid separator and an ammonia recoverytower. The method comprises the steps as follows: pulverizing straw, presoaking the straw by water to achieve 10 to 60 percent of moisture content, placing the straw into the reaction tank, outputtingthe ammonia liquid (liquid ammonia or ammonia water) to the reaction tank and the ammonia liquid buffer tank in sequence by the plunger pump, achieving the fluidization of the straw along with the time gradient through the ammonia circulation and ammonia flow adjustment, meanwhile, heating the reaction tank to 70 to 100 DEG C by steam, discharging the ammonia liquid from the reaction tank after 2to 15 min reaction, exploding the material to the material reception tank, sending the material to the solid-liquid separator for separating after cooled, collecting solid products and liquid products, and recovering reacted ammonia. The whole set of device is more close to the target which is applicable to the practical production, and has the greater application potential.
Description
Technical field
The utility model belongs to the biological chemical field of stalk, and particularly a kind of gradient fluidisation ammonia circulation blasting procedure is mainly used in the preliminary treatment of various plants stalks such as maize straw, straw to the device of straw removing crystallization.
Background technology
Undressed stalk is difficult to by microorganism and enzyme hydrolysis, mainly is because the structure of the lignocellulose of formation stalk cell wall is comparatively complicated.Lignocellulose mainly comprises cellulose, hemicellulose, three kinds of components of lignin, and hemicellulose and lignin are formed network structure by covalent bond, with the cellulosic molecule embedding wherein, makes enzyme be difficult for contacting with cellulosic molecule.Many cellulosic molecules connect the common crystalline texture of forming by hydrogen bond simultaneously, make cellulosic polymer demonstrate rigidity and height water-insoluble, have increased the difficulty of enzymolysis.Therefore efficiently utilize the key of straw component to be by stalk is carried out preliminary treatment, part is removed compositions such as lignin and hemicellulose, destroy cellulosic crystalline texture, increase the porous of biological material, increase the contact area of enzyme and raw material, improve the accessibility of enzyme, thereby improve the enzymolysis efficiency of stalk.
By various preprocess methods, improve biomass cellulose sugar conversion ratio and be used widely in each field.Present preprocess method comprises the alkali treatment method, diluted acid facture, the quick-fried facture of vapour etc.There is following problem in these methods aspect technical and the economy: (1) makes part sugar degraded in processing procedure, produces acids, aldehyde material, reduce sugared rate, suppress follow-up sweat; (2) dispose with chemical method, be difficult for from from product, reclaiming chemicals; (3) residual chemicals can suppress follow-up sweat; (4) behind preliminary treatment and the enzymolysis sugared rate low, infeasible economically.
Bioenergy transformation experiment chamber, Michigan State University under U.S. Bruce professor E.Dale leads, be engaged in the research of cellulose preliminary treatment direction for a long time, they develop a kind of technology---ammonia fiber explosion pretreating process that utilizes the liquefied ammonia realization to the stalk explosion treatment the eighties in last century, be called for short AFEX technology, and be in world lead level aspect the integration of the design of AFEX technology and optimization, parameter control and total system always.This technology is used high-pressure liquid ammonia and stalk reaction, heating and decompression suddenly after insulation a period of time, ammonia becomes gaseous state by liquid state realizes that thereby the stalk explosion reaches pretreating effect, it has intact, the recyclable almost advantages such as nitrogenous source when all residual micro-ammonia can be used as sugar fermentation after ammonia, the explosion of few generation fermentation inhibitor, cellulose and hemicellulose, is a kind of up-and-coming stalk pretreating process.But, this technology also exist the liquefied ammonia cost higher, reach that the required energy consumption of condition of high voltage is big, the equipment investment of ammonia reclaiming process and energy consumption is big, relatively poor to hardwood and cork treatment effect, along with the shortcomings such as rising process result degrades of content of lignin in the stalk.
Summary of the invention
The purpose of this utility model is at the deficiency of existing AFEX PROCESS FOR TREATMENT stalk, and a kind of improved device that utilizes gradient fluidisation ammonia circulation blasting procedure to the straw removing crystallization is provided, for the development and use of biomass energy provide a new approach.This installs with quiet stagnant liquefied ammonia in ammoniacal liquor (liquefied ammonia or ammoniacal liquor) the replacement AFEX technology of fluidisation to improve reaction efficiency, can realize fluidisation degree graded in time by the flow of regulating ammonia, thereby partly replacing liquefied ammonia with ammoniacal liquor reduces cost, make the more target of convergence production application of package unit, bigger application potential is arranged.
The gradient fluidisation ammonia circulation blasting procedure that the utility model provides comprises stalk crasher, ammonia bottle, plunger displacement pump, ammoniacal liquor explosion retort, ammoniacal liquor surge tank, material receiving tank, solid-liquid separator and ammonia recovery tower to the device of straw removing crystallization.
Ammoniacal liquor explosion retort upper end is connected with the ammonia bottle via plunger displacement pump, the lower end is connected by pipeline with the upper end of ammoniacal liquor surge tank, and be connected with material receiving tank under it by explosive valve, ammoniacal liquor surge tank lower end is connected by pipeline with plunger displacement pump, and the material receiving tank is connected with the ammonia recovery tower with solid-liquid separator.
Use the utility model specifically to may further comprise the steps:
After 1 pulverizing of stalk usefulness pulverizer and preimpregnation, put into ammoniacal liquor explosion retort 4.Be delivered to retort 4 with plunger displacement pump 3 ammoniacal liquor (liquefied ammonia or ammoniacal liquor) by 10-50ml ammoniacal liquor/(g dry straw) from ammonia bottle 2, the ammoniacal liquor of 2-10ml ammoniacal liquor/(g dry straw) is delivered to ammoniacal liquor surge tank 5, makes circulation ammonia load (the ammoniacal liquor quality that is added and the ratio of dry straw quality) reach 12-60ml ammoniacal liquor/(g dry straw).Control valve, provide power by plunger displacement pump 3, make constantly unidirectional circulating between plunger displacement pump 3, ammoniacal liquor explosion retort 4 and ammoniacal liquor surge tank 5 of ammonia, thereby the fluidisation of material in the realization response jar 4, the circulation ammonia flow is 10-50ml ammoniacal liquor/(g dry straw min), and can realize fluidisation degree graded in time by the flow of regulating ammonia.In the chuck of retort 4, feed saturated vapor simultaneously and be heated to reaction temperature 70-100 ℃, reaction pressure 3.2-6.2MPa, reaction and insulation 2-15min.After reaction finished, plunger displacement pump 3 quit work, and control valve to ammoniacal liquor surge tank 5, is closed the valve between two jars with the emission intensity in the ammoniacal liquor explosion retort 4 then, opens explosive valve, the realization explosion of volatilizing rapidly of the residual ammonia in the stalk.Material in the retort 4 enters material receiving tank 6 under differential pressure action, send into after the cooling and separate in the solid-liquid separator 7 and collection gained solid product and fluid product.Ammoniacal liquor in the collection ammoniacal liquor surge tank 5 and the ammonia in the material receiving tank 6 feed the recycling that realizes ammonia in the ammonia recovery tower 8.Feed the residual ammonia in nitrogen blow-off's pipeline and ammoniacal liquor explosion retort 4, ammoniacal liquor surge tank 5, the material receiving tank 6.
All steam pipeworks in above-mentioned and ammoniacal liquor explosion retort 4, ammoniacal liquor surge tank 5, ammonia recovery tower 8 are all realized insulation with the rock wool parcel.The outside of ammoniacal liquor explosion retort has chuck, and steam feeds in the chuck ammoniacal liquor explosion retort is heated.
In the retort 4 in above-mentioned and the connecting line of ammoniacal liquor surge tank 5, retort 4 exits are provided with filter screen, together flow out with circulation ammonia to stop material.
Operating temperature is respectively 10～40 ℃ and 120～140 ℃ at the bottom of the cat head operating temperature of the ammonia recovery tower 8 in above-mentioned and the tower.
The utility model proposes the device of a kind of novel gradient fluidisation ammonia circulation blasting procedure to the straw removing crystallization.This covering device has guaranteed that material fully reacts with ammonia under fluidized state, and can realize fluidisation degree graded in time, and quiet stagnant liquefied ammonia has improved reaction efficiency in the AFEX technology.Partly replace liquefied ammonia to react the economic performance that has also improved technology with ammoniacal liquor.This method processing cycle is short, the economic efficacy height, and the accessibility of the enzyme of the material of handling greatly improves, thereby enzymatic hydrolyzation is improved, and package unit is the target of convergence production application more, and bigger application potential is arranged.
Description of drawings
Fig. 1 is a technological process device schematic diagram of the present utility model.
The specific embodiment
In conjunction with the accompanying drawings the utility model is further described.
As shown in the figure, 1. pulverizer, 2. ammonia bottle, 3. plunger displacement pump, 4. ammoniacal liquor explosion retort, 5. ammoniacal liquor surge tank, 6. material receiving tank, 7. solid-liquid separator, 8. ammonia recovery tower.
Ammoniacal liquor explosion retort 4 is connected with plunger displacement pump 3, ammoniacal liquor surge tank 5 and material receiving tank 6 respectively, main effect be by charging aperture receive after pulverizing through pulverizer 1 stalk and from the ammoniacal liquor of plunger displacement pump 3, ammoniacal liquor and stalk react therein; Ammoniacal liquor enters ammoniacal liquor surge tank 5 after flowing out retort, is carried back retort 4 by plunger displacement pump 3 again, thereby realizes the circulation of ammonia; Reaction finish the back by explosive valve with stalk from retort 4 explosions to material receiving tank 6.
Operating procedure is as follows:
1) pulverize preimpregnation, straw is crushed to particle diameter in stalk crasher 1 be 1-20mm, and being dipped into moisture in advance with clear water then is 10-60%;
2) reinforced, the by-pass valve control switch adds ammoniacal liquor explosion retort 4 with stalk by charging aperture;
3) logical ammonia, with plunger displacement pump 3 from ammonia bottle 2 is that the ammoniacal liquor (liquefied ammonia or ammoniacal liquor) of 10-50ml ammoniacal liquor/(g dry straw) is delivered to retort 4 with ammonia load, the ammoniacal liquor of 2-10ml ammoniacal liquor/(g dry straw) is delivered to ammoniacal liquor surge tank 5, makes circulation ammonia load reach 12-60ml ammoniacal liquor/(g dry straw);
4) fluidisation, control valve, provide power by plunger displacement pump 3, make constantly unidirectional circulating between plunger displacement pump 3, ammoniacal liquor explosion retort 4 and ammoniacal liquor surge tank 5 of ammonia, thereby the fluidisation of material in the realization response jar 4, the circulation ammonia flow is 10-50ml ammoniacal liquor/(g dry straw min), and can realize fluidisation degree graded in time by the flow of regulating ammonia;
5) heating feeds the chuck of retort 4 with steam, and material and ammonia are heated to 70-100 ℃;
6) reaction, material and ammoniacal liquor reaction and be incubated 2-15min under 70-100 ℃, the condition of 3.2-6.2MPa, 10-50ml ammoniacal liquor/(g dry straw), 10-50ml ammoniacal liquor/(g dry straw min);
7) discharge opeing, after reaction finished, plunger displacement pump 3 quit work, and control valve to ammoniacal liquor surge tank 5, is closed the valve between two jars with the emission intensity in the ammoniacal liquor explosion retort 4 then;
8) ammonia is quick-fried, opens explosive valve, the realization explosion of volatilizing rapidly of the residual ammonia in the stalk.Material in the retort 4 enters material receiving tank 6 under differential pressure action;
9) Separation of Solid and Liquid is sent in the solid-liquid separator 7 after the material cooling, separates and collection gained solid product and fluid product;
10) ammonia reclaims, and ammoniacal liquor in the collection ammoniacal liquor surge tank 5 and the ammonia in the material receiving tank 6 feed the recycling that realizes ammonia in the ammonia recovery tower 8;
11) blow down, feed the residual ammonia in nitrogen blow-off's pipeline and ammoniacal liquor explosion retort 4, ammoniacal liquor surge tank 5, the material receiving tank 6;
12) clean, water pipe cleans ammoniacal liquor explosion retort 4 and material receiving tank 6.
Dried maize straw is crushed to particle diameter is about 8-10mm in stalk crasher, it is 60% that water is dipped into moisture in advance, put into ammoniacal liquor explosion retort, with plunger displacement pump the liquefied ammonia of 25ml ammoniacal liquor/(g dry straw) is delivered to ammoniacal liquor explosion retort, the liquefied ammonia of 5ml ammoniacal liquor/(g dry straw) is delivered to the ammoniacal liquor surge tank, makes circulation ammonia load reach 30ml ammoniacal liquor/(g dry straw).Control valve, provide power by plunger displacement pump, liquefied ammonia is constantly circulated between plunger displacement pump, ammoniacal liquor explosion retort and ammoniacal liquor surge tank, and the circulation ammonia flow is 25ml ammoniacal liquor/(g dry straw min), and the interior stalk material of retort this moment is in the aggregative fluidization state.In reactor jacket, feed steam material is heated to 90 ℃.Behind the reaction 5min, plunger displacement pump quits work, and control valve is disposed to the ammoniacal liquor surge tank with the liquefied ammonia in the ammoniacal liquor explosion retort, closes the valve between two jars then.Open explosive valve, the realization explosion of volatilizing rapidly of the residual ammonia in the stalk.Material in the retort enters the material receiving tank under differential pressure action, send into the solid-liquid separator separation after the cooling and collect gained solid product and fluid product.Ammoniacal liquor in the collection ammoniacal liquor surge tank and the ammonia in the material receiving tank enter the recycling that realizes ammonia in the ammonia recovery tower.Feed the residual ammonia in nitrogen blow-off's pipeline and ammoniacal liquor explosion retort, ammoniacal liquor surge tank, the material receiving tank, and water pipe cleans ammoniacal liquor explosion retort and material receiving tank.The relative crystallinity of the stalk after the processing has reduced by 17.3%, enzymolysis 24h, and enzymatic hydrolyzation reaches 75.3%, and enzymolysis 48h reaches 94.5%.
Embodiment 2
Dried maize straw is crushed to particle diameter in stalk crasher be 1-3mm, it is 40% that water is dipped into moisture in advance, put into ammoniacal liquor explosion retort, with plunger displacement pump the ammoniacal liquor of 40ml ammoniacal liquor/(g dry straw) is delivered to ammoniacal liquor explosion retort, the ammoniacal liquor of 8ml ammoniacal liquor/(g dry straw) is delivered to the ammoniacal liquor surge tank, makes circulation ammonia load reach 48ml ammoniacal liquor/(g dry straw).Control valve, provide power by plunger displacement pump, make constantly unidirectional circulating between plunger displacement pump, ammoniacal liquor explosion retort and ammoniacal liquor surge tank of ammoniacal liquor, the circulation ammonia flow is 37.5ml ammoniacal liquor/(g dry straw min), and the interior stalk material of retort this moment is in even fluidized state.In reactor jacket, feed steam material is heated to 100 ℃.Behind the reaction 5min, the circulation ammonia flow is decreased to 25ml ammoniacal liquor/(g dry straw min) by 37.5ml ammoniacal liquor/(g dry straw min), continues reaction 5min.After reaction finished, plunger displacement pump quit work, and control valve is disposed to the ammoniacal liquor surge tank with the ammoniacal liquor in the ammoniacal liquor explosion retort, closes the valve between two jars then.Open explosive valve, the realization explosion of volatilizing rapidly of the residual ammonia in the stalk.Material in the retort enters the material receiving tank under differential pressure action, send into the solid-liquid separator separation after the cooling and collect gained solid product and fluid product.Ammoniacal liquor in the collection ammoniacal liquor surge tank and the ammonia in the material receiving tank enter the recycling that realizes ammonia in the ammonia recovery tower.Feed the residual ammonia in nitrogen blow-off's pipeline and ammoniacal liquor explosion retort, ammoniacal liquor surge tank, the material receiving tank, and water pipe cleans ammoniacal liquor explosion retort and material receiving tank.The relative crystallinity of the stalk after the processing has reduced by 21.7%, enzymolysis 24h, and enzymatic hydrolyzation reaches 79.7%, and enzymolysis 48h reaches 98.5%.
Claims (3)
1, a kind of gradient fluidisation ammonia circulation blasting procedure is characterized in that to the device of straw removing crystallization it comprises stalk crasher, ammonia bottle, plunger displacement pump, ammoniacal liquor explosion retort, ammoniacal liquor surge tank, material receiving tank, solid-liquid separator and ammonia recovery tower; Ammoniacal liquor explosion retort upper end is connected with the ammonia bottle via plunger displacement pump, the lower end is connected by pipeline with the upper end of ammoniacal liquor surge tank, and be connected with material receiving tank under it by explosive valve, ammoniacal liquor surge tank lower end is connected by pipeline with plunger displacement pump, and the material receiving tank is connected with the ammonia recovery tower with solid-liquid separator.
2, device according to claim 1 is characterized in that, in the connecting line of described retort and ammoniacal liquor surge tank, the retort exit is provided with filter screen.
3, device according to claim 1 is characterized in that, the outside of described ammoniacal liquor explosion retort has chuck and rock wool heat-preservation layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009200977410U CN201428085Y (en) | 2009-07-13 | 2009-07-13 | Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009200977410U CN201428085Y (en) | 2009-07-13 | 2009-07-13 | Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201428085Y true CN201428085Y (en) | 2010-03-24 |
Family
ID=42031816
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009200977410U Expired - Fee Related CN201428085Y (en) | 2009-07-13 | 2009-07-13 | Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201428085Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101230545B (en) * | 2008-02-26 | 2012-02-15 | 侯梦斌 | Method for preparing slurry by blast process |
-
2009
- 2009-07-13 CN CN2009200977410U patent/CN201428085Y/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101230545B (en) * | 2008-02-26 | 2012-02-15 | 侯梦斌 | Method for preparing slurry by blast process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8017820B2 (en) | Continuous flowing pre-treatment system with steam recovery | |
| US20190106718A1 (en) | Lignocellulosic conversion process comprising sulfur dioxide and/or sulfurous acid pretreatment | |
| US20100330638A1 (en) | Thermochemical Treatment of Lignocellulosics for the Production of Ethanol | |
| CN101608412B (en) | Decrystallization method for plant straw by microwave-steam explosion synchronous coupling method | |
| US20120301928A1 (en) | Preprocessing method of hydrolyzing lignocellulosic biomass and methods of manufacturing sugar compound and bioethanol from biomass processed using the preprocessing method | |
| CN102261004B (en) | Biological-chemical combined pretreatment method of lignocellulosic materials | |
| CA2817389A1 (en) | Continuously fed biomass pretreatment process for a packed bed reactor | |
| US9102965B2 (en) | Saccharide-solution producing apparatus, fermentation system, saccharide-solution producing method, and fermentation method | |
| CN101942382B (en) | Device and method for producing butanol by fermenting straw dilute acid hydrolyzed pentaglucose | |
| CN103243136A (en) | Method for improving enzymolysis saccharification efficiency of lignocellulose | |
| WO2013103138A1 (en) | Biomass saccharification method and device, method and device for producing sugar, and method and device for producing ethanol | |
| Wang et al. | Bioconversion of corn fiber to bioethanol: Status and perspectives | |
| CN106834360A (en) | The preprocess method and device of a kind of lignocellulosic material | |
| CN102827898B (en) | Method for vacuum-assisted hydrothermal pretreatment of biomass | |
| CN103924469A (en) | Method for removing lignin | |
| CN201428085Y (en) | Device for performing crystallization removing to plant straw through adopting circulating explosion method of gradient fluidized ammonia | |
| CN102720083A (en) | Method for pretreating biomass by ball milling coupled with microwave | |
| CN101613972B (en) | Method for removing crystallization of plant stalks by gradient fluidized ammonia circulating explosion method | |
| CN106834361A (en) | The method that stalk produces cellulosic ethanol | |
| BR112021012936A2 (en) | METHOD OF TREATMENT OF A LIGNOCELLULOSIC BIOMASS | |
| CN102660587A (en) | Method for pretreating lignocellulose raw material continuously/intermittently under normal pressure by using calcium chloride solution | |
| CN201428086Y (en) | Device for performing crystallization removing to plant straw through adopting method of microwave-steam explosion synchronous coupling | |
| Chakraborty et al. | Production of cellulosic fuels | |
| Tinôco | Biotechnology Development of Bioethanol from Sweet Sorghum Bagasse | |
| US20230340543A1 (en) | Converting lignocellulosic feedstock to fuel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100324 Termination date: 20120713 |