CN105669419A - Method for separation of sugar acid from corn straw acidolysis solution by sequential simulant moving bed - Google Patents
Method for separation of sugar acid from corn straw acidolysis solution by sequential simulant moving bed Download PDFInfo
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Abstract
The invention relates to a method for separation of sugar acid from a corn straw acidolysis solution by a sequential simulant moving bed. The method specifically includes: separation of the corn straw acidolysis solution by sequential simulant moving bed chromatography separation equipment in three stages: a separation stage, which consists of connecting 8 chromatographic columns in series, pumping out the liquid from a third column by a circulating pump therebelow and injecting the liquid into a fourth column, injecting the liquid from the fourth column into a fifth column, and repeating the operation cyclically in order; a desorption stage, which consists of injecting a desorption agent from the upper part of a first column, and discharging a sulfuric acid solution at the bottom of a sixth column; and a feed desorption stage, which consists of injecting a desorption agent from the upper part of the first column, injecting the corn straw acidolysis solution from the upper part of the fifth chromatographic column, discharging a sugar solution from the bottom of the first column, and discharging a sulfuric acid solution from the bottom of the sixth chromatographic column, with the separated sulfuric acid solution having a concentration of 210mg/mL-320mg/mL and the sugar solution having a concentration of 20mg/mL-41mg/mL; concentration and recovery of the sulfuric acid solution; and filtering and concentration of the sugar solution. According to the method provided by the invention, the separated sulfuric acid and sugar solution have a high concentration, thus solving the problems of difficult sulfuric acid recovery and high cost in corn straw reutilization.
Description
One, technical field
What the present invention relates to is the isolation technique of sulfuric acid and sugar liquid in maize straw acid hydrolysis solution, is specifically related to the method for saccharic acid in sequential simulated moving bed separating corn stalk acid hydrolysis solution.
Two, background technology
China is a large agricultural country, and all kinds of agronomic crop fibre resource is very abundant, and only stalk one just reaches more than 700,000,000 tons every year, wherein maize straw about 2.2 hundred million tons. But at present except the feed that sub-fraction is used as ruminating animal, rest part is burnt mainly with fuel, causes Air seriously polluted. Containing a large amount of Mierocrystalline celluloses and hemicellulose in maize straw, transform saccharogenesis by number of ways, as the source of fermentation industry low cost feedstock.
Maize straw is refined sugar based on sulphuric acid hydrolysis and enzyme liberating method, and wherein, because of enzyme class cost height, production efficiency is low, so the not extensive hydrolysis for maize straw of enzyme liberating method is applied. Sulphuric acid hydrolysis maize straw all has clear superiority in technical process, production cost and total reducing sugar receipts rate, can large-scale application in the pre-treatment of maize straw. But the removal of sulfuric acid is a difficult problem for puzzlement Business survival and development in the method always, ion-exchange-resin process is utilized to be adsorbed by the sulfuric acid in corn stalk hydrolysis, there is cost height, inefficient problem, the washing fluid discharge of regenerating ion exchange resin simultaneously can cause a large amount of pollutions. Therefore, effectively being reclaimed by the sulfuric acid in maize straw acid hydrolysis solution, and control its cost recovery, the utilization that maize straw acid hydrolysis solution carries out high added value simultaneously is the main research contents during maize straw recycles.
Chinese patent 201210005679.4 discloses the sugar of a kind of lignocellulose hydrolysate, acid, salt separation method, literary composition is mentioned utilizing and simulation moving-bed hydrolyzed solution is carried out saccharic acid separation, during separation, mineral acid, salt are fast component, sugar, acetic acid are slow component, acetic acid and sugar are not separated completely, and do not list concrete simulation moving-bed separating technology and condition.
Li Xun etc. report the research [solar energy journal of the saccharic acid in simulation moving-bed ion exclusion chromatography separation hydrolyzed solution, 2005, 29 (6): 747-751], biomass hydrolysate is carried out saccharic acid separation for utilizing 8 post 4 district's continuous simulation moving-beds by its main contents, in raw material, the concentration of sulfuric acid is 12%～15%, in extracting solution, sugar concentration is 1.5%～2.0%, the simulation moving-bed separating technology adopted is traditional 4 district's patterns, this pattern is continuously feeding, continuous wash-out, the time acting on separating substances is shorter, there is production efficiency low, the problems such as solution cost recovery height.Due to this kind of restriction, in raw material, amount of dry matter is difficult to improve, if raising can cause being separated rear product purity and the decline of receipts rate.
Three, summary of the invention
Having it is an object of the present invention to provide the method for saccharic acid in sequential simulated moving bed separating corn stalk acid hydrolysis solution, in this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is applicable to solve traditional simulation moving-bed separating technology and carries out the solution cost recovery height that saccharic acid separation exists, the problem that production efficiency is low.
In order to realize above-mentioned purpose, the concrete technical scheme that the present invention adopts is as follows: the method for saccharic acid in this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, taking maize straw acid hydrolysis solution as raw material, adopt sequential simulated moving bed separating device separation sulfuric acid and sugar liquid, sulfuric acid content 500mg/ml～700mg/ml, sugar liquid hold-up 60mg/ml～80mg/ml in maize straw acid hydrolysis solution; Specific as follows:
A, sequential simulated moving bed separation: described maize straw acid hydrolysis solution is separated by sequential type simulated moving bed chromatography equipment, sepn process one-period comprises 8 steps, each step comprises three phases, first stage is separation phase, 8 root chromatogram columns are connected in series, being extracted out by liquid in post by the recycle pump being arranged under the 3rd post and inject the 4th post, in the 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post; Phase III is charging desorption phase, enters strippant on the 1st post top, and the 5th root chromatogram column top enters described maize straw acid hydrolysis solution, releases sugar soln, release sulphuric acid soln under the 6th root chromatogram column under the 1st post. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state. The sulphuric acid soln concentration that obtains of separation is 210mg/mL～320mg/mL, purity is 93%～98%, and sugar soln concentration is 20mg/mL～41mg/mL, purity 93%～96%;
B, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through a step is carried out rotary evaporation process, temperature 50 DEG C～65 DEG C, obtains concentrated solution, and concentrated solution concentration is 500mg/mL～550mg/mL;
C, sugar soln filter: filtered by obtained for a step sugar soln micron-rated filter, the yellow liquid of obtained clarification;
D, sugar soln are concentrated: obtained for step c sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification.
The preparation method of maize straw acid hydrolysis solution in such scheme:
The preparation of the first step, maize straw acid hydrolysis solution: maize straw is dried, pulverized 40 order sieves, take certain mass maize straw, the sulphuric acid soln of volumetric concentration 3% is added according to the ratio of solid-liquid ratio 1:50, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution;
2nd step, the maize straw acid hydrolysis solution filtration the first step obtained with filter paper, obtain clarification dark brown liquid, and utilizes Rotary Evaporators to be concentrated to solution sulfuric acid content 500mg/ml～700mg/ml, sugar liquid hold-up 60mg/ml～80mg/ml.
The sulphuric acid concentration liquid dilution that in such scheme, step b obtains obtains the sulphuric acid soln of volumetric concentration 3%, is recycled and reused in the first step prepared by maize straw acid hydrolysis solution.
In separation sequential simulated moving bed in such scheme, sorbent material is Zeo-karb UBK08, IR120H+、IR118H+、IR120Na+Or AMBERJETC1H+In any one; Strippant is deionized water, and separation temperature is 50 DEG C～55 DEG C, and first stage internal circulating load is 410～550mL; Subordinate phase, strippant flow is 23～45mL/min, and desorption time is 110～160s; Phase III, strippant flow is 30～45mL/min, and charging amount is 35～50mL/min, charging and desorption time is 120～180s.
Useful effect:
1, the core technology of the present invention is sulfuric acid and sugar liquid technology in sequential simulated moving bed separating corn stalk acid hydrolysis solution, with relatively high separation, sulfuric acid is separated with sugar liquid, raw materials used sulfuric acid concentration reaches 50%～80%, sugar concentration is 6%～8%, exceeding 3～5 times compared with the sulfuric acid concentration in the biomass materials used such as Li Xun, the treatment capacity of technique obviously increases; The technique [solar energy journal, 2005,29 (6): 747-751] that Li Xun etc. report according to it be separated after sulfuric acid concentration be up to 7%, sugar concentration is up to 2%, sulfuric acid and sugar liquid purity and receipts rate reach 93%. Process acts of the present invention is longer in the time of separating substances, and the sulfuric acid concentration after separation is up to 31.8%, purity can reach 97.8%, and receipts rate can reach 98%, and sugar soln concentration is up to 4.05%, purity can reach 95%, and receipts rate can reach 97%; Therefore, this technique can save a large amount of energy in follow-up concentration, and sulfuric acid is higher with receipts rate and the purity of sugar liquid, solves a recovery difficult problem for sulfuric acid in maize straw recycling, has process simplicity, the characteristic that technique cost savings etc. are distinct.
2, the present invention adopt sequential simulated moving bed to sulfuric acid in maize straw acid hydrolysis solution with sugar liquid be separated, the receipts rate obtaining sulphuric acid soln is 93%～98%, and sugar soln receipts rate is 94%～97%. Good separating effect, receipts rate height, is easy to suitability for industrialized production and amplifies.
Four, embodiment
The present invention is described further below:
Embodiment 1:
In this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is as follows:
The preparation of a, maize straw acid hydrolysis solution: maize straw is dried, pulverized 40 order sieves, take 2g corn stalk powder, add the sulphuric acid soln 100mL of volumetric concentration 3%, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution.
B, maize straw acid hydrolysis solution filtration a step obtained with filter paper, obtain clarification dark brown liquid, and utilize Rotary Evaporators to be concentrated to solution sulfuric acid concentration 519.4mg/mL, sugar concentration 61.49mg/mL.
C, sequential simulated moving bed separation: the maize straw acid hydrolysis solution after process is separated by sequential type simulated moving bed chromatography equipment, sorbent material is Zeo-karb UBK08; Strippant is deionized water, separation temperature is 50 DEG C, sepn process one-period comprises 8 steps, each step comprises three phases, and the first stage is separation phase, and 8 root chromatogram columns are connected in series, by the recycle pump being arranged under the 3rd post liquid in post extracted out and inject the 4th post, in 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively, and internal circulating load is 410mL;Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post, and strippant flow is 23.5mL/min, and desorption time is 112s; Phase III is charging desorption phase, strippant is entered on the 1st post top, 5th root chromatogram column top enters b step gained maize straw acid hydrolysis solution, sugar soln is released under 1st post, sulphuric acid soln is released under 6th root chromatogram column, strippant flow is 30.5mL/min, and charging amount is 42.2mL/min, charging and desorption time is 180s. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state. The sulphuric acid soln concentration that obtains of separation is 230mg/mL, purity is 93.1%, and receipts rate is 93.5%, and sugar soln concentration is 24.8mg/mL, purity 95.2%, and receipts rate is 94.2%;
D, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through step c is carried out rotary evaporation process, temperature 55 DEG C, obtains concentrated solution, then is repeated maize straw acidolysis experiment;
E, sugar soln filter: filtered by obtained for step c sugar soln micron-rated filter, the yellow liquid of obtained clarification;
F, sugar soln are concentrated: obtained for step e sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification;
Embodiment 2:
In this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is as follows:
The preparation of a, maize straw acid hydrolysis solution: maize straw is dried, pulverizes, take certain mass maize straw, the sulphuric acid soln of volumetric concentration 3% is added according to solid-liquid ratio 1:50 ratio, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution.
B, maize straw acid hydrolysis solution filtration a step obtained with filter paper, obtain clarification dark brown liquid, and utilize Rotary Evaporators to be concentrated to solution sulfuric acid concentration 562.3mg/mL, sugar concentration 65.8mg/mL.
C, sequential simulated moving bed separation: the maize straw acid hydrolysis solution after process is separated by sequential type simulated moving bed chromatography equipment, sorbent material is Zeo-karb IR120H+; Strippant is deionized water, separation temperature is 55 DEG C, sepn process one-period comprises 8 steps, each step comprises three phases, and the first stage is separation phase, and 8 root chromatogram columns are connected in series, by the recycle pump being arranged under the 3rd post liquid in post extracted out and inject the 4th post, in 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively, and internal circulating load is 435mL; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post, and strippant flow is 25.1mL/min, and desorption time is 123s; Phase III is charging desorption phase, strippant is entered on the 1st post top, 5th root chromatogram column top enters b step gained maize straw acid hydrolysis solution, sugar soln is released under 1st post, sulphuric acid soln is released under 6th root chromatogram column, strippant flow is 30.1mL/min, and charging amount is 43.5mL/min, charging and desorption time is 179s. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state.The sulphuric acid soln concentration that obtains of separation is 241mg/mL, purity is 94%, and receipts rate is 95.2%, and sugar soln concentration is 26.3mg/mL, purity 93.5%, and receipts rate is 94.6%;
D, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through step c is carried out rotary evaporation process, temperature 55 DEG C, obtains concentrated solution, then is repeated maize straw acidolysis experiment;
E, sugar soln filter: filtered by obtained for step c sugar soln micron-rated filter, the yellow liquid of obtained clarification;
F, sugar soln are concentrated: obtained for step e sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification;
Embodiment 3:
In this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is as follows:
The preparation of a, maize straw acid hydrolysis solution: maize straw is dried, pulverizes, take certain mass maize straw, the sulphuric acid soln of volumetric concentration 3% is added according to solid-liquid ratio 1:50 ratio, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution.
B, maize straw acid hydrolysis solution filtration a step obtained with filter paper, obtain clarification dark brown liquid, and utilize Rotary Evaporators to be concentrated to solution sulfuric acid concentration 616.1mg/mL, sugar concentration 70.2mg/mL.
C, sequential simulated moving bed separation: the maize straw acid hydrolysis solution after process is separated by sequential type simulated moving bed chromatography equipment, sorbent material is Zeo-karb IR118H+; Strippant is deionized water, separation temperature is 55 DEG C, sepn process one-period comprises 8 steps, each step comprises three phases, and the first stage is separation phase, and 8 root chromatogram columns are connected in series, by the recycle pump being arranged under the 3rd post liquid in post extracted out and inject the 4th post, in 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively, and internal circulating load is 428mL; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post, and strippant flow is 24.5mL/min, and desorption time is 112s; Phase III is charging desorption phase, strippant is entered on the 1st post top, 5th root chromatogram column top enters b step gained maize straw acid hydrolysis solution, sugar soln is released under 1st post, sulphuric acid soln is released under 6th root chromatogram column, strippant flow is 34.5mL/min, and charging amount is 36.4mL/min, charging and desorption time is 127s. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state. The sulphuric acid soln concentration that obtains of separation is 318.6mg/mL, purity is 97.8%, and receipts rate is 98%, and sugar soln concentration is 40.5mg/mL, purity 95%, and receipts rate is 97%;
D, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through step c is carried out rotary evaporation process, temperature 55 DEG C, obtains concentrated solution, then is repeated maize straw acidolysis experiment;
E, sugar soln filter: filtered by obtained for step c sugar soln micron-rated filter, the yellow liquid of obtained clarification;
F, sugar soln are concentrated: obtained for step e sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification;
Embodiment 4:
In this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is as follows:
The preparation of a, maize straw acid hydrolysis solution: maize straw is dried, pulverizes, take certain mass maize straw, the sulphuric acid soln of volumetric concentration 3% is added according to solid-liquid ratio 1:50 ratio, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution.
B, maize straw acid hydrolysis solution filtration a step obtained with filter paper, obtain clarification dark brown liquid, and utilize Rotary Evaporators to be concentrated to solution sulfuric acid concentration 546.8mg/mL, sugar concentration 63.4mg/mL.
C, sequential simulated moving bed separation: the maize straw acid hydrolysis solution after process is separated by sequential type simulated moving bed chromatography equipment, sorbent material is Zeo-karb IR120Na+; Strippant is deionized water, separation temperature is 52 DEG C, sepn process one-period comprises 8 steps, each step comprises three phases, and the first stage is separation phase, and 8 root chromatogram columns are connected in series, by the recycle pump being arranged under the 3rd post liquid in post extracted out and inject the 4th post, in 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively, and internal circulating load is 430mL; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post, and strippant flow is 25.8mL/min, and desorption time is 131s; Phase III is charging desorption phase, strippant is entered on the 1st post top, 5th root chromatogram column top enters b step gained maize straw acid hydrolysis solution, sugar soln is released under 1st post, sulphuric acid soln is released under 6th root chromatogram column, strippant flow is 35.6mL/min, and charging amount is 40.5mL/min, charging and desorption time is 156s. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state. The sulphuric acid soln concentration that obtains of separation is 214mg/mL, purity is 95.2%, and receipts rate is 95.2%, and sugar soln concentration is 23.4mg/mL, purity 94.6%, and receipts rate is 94.8%;
D, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through step c is carried out rotary evaporation process, temperature 55 DEG C, obtains concentrated solution, then is repeated maize straw acidolysis experiment;
E, sugar soln filter: filtered by obtained for step c sugar soln micron-rated filter, the yellow liquid of obtained clarification;
F, sugar soln are concentrated: obtained for step e sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification;
Embodiment 5:
In this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, the method for saccharic acid is as follows:
The preparation of a, maize straw acid hydrolysis solution: maize straw is dried, pulverizes, take certain mass maize straw, the sulphuric acid soln of volumetric concentration 3% is added according to solid-liquid ratio 1:50 ratio, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution.
B, maize straw acid hydrolysis solution filtration a step obtained with filter paper, obtain clarification dark brown liquid, and utilize Rotary Evaporators to be concentrated to solution sulfuric acid concentration 635.4mg/mL, sugar concentration 73.5mg/mL.
C, sequential simulated moving bed separation: the maize straw acid hydrolysis solution after process is separated by sequential type simulated moving bed chromatography equipment, sorbent material is Zeo-karb AMBERJETC1H+; Strippant is deionized water, separation temperature is 55 DEG C, sepn process one-period comprises 8 steps, each step comprises three phases, and the first stage is separation phase, and 8 root chromatogram columns are connected in series, by the recycle pump being arranged under the 3rd post liquid in post extracted out and inject the 4th post, in 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively, and internal circulating load is 550mL; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post, and strippant flow is 32.5mL/min, and desorption time is 146s; Phase III is charging desorption phase, strippant is entered on the 1st post top, 5th root chromatogram column top enters b step gained maize straw acid hydrolysis solution, sugar soln is released under 1st post, sulphuric acid soln is released under 6th root chromatogram column, strippant flow is 32.5mL/min, and charging amount is 41.3mL/min, charging and desorption time is 162s. After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state. The sulphuric acid soln concentration that obtains of separation is 264mg/mL, purity is 93.4%, and receipts rate is 94.3%, and sugar soln concentration is 32.4mg/mL, purity 94.9%, and receipts rate is 96.2%;
D, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through step c is carried out rotary evaporation process, temperature 55 DEG C, obtains concentrated solution, then is repeated maize straw acidolysis experiment;
E, sugar soln filter: filtered by obtained for step c sugar soln micron-rated filter, the yellow liquid of obtained clarification;
F, sugar soln are concentrated: obtained for step e sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification.
In the present invention, solid-liquid ratio is mass volume ratio.
Claims (4)
1. the method for saccharic acid in a sequential simulated moving bed separating corn stalk acid hydrolysis solution, it is characterized in that: the method for saccharic acid in this kind of sequential simulated moving bed separating corn stalk acid hydrolysis solution, taking maize straw acid hydrolysis solution as raw material, adopt sequential simulated moving bed separating device separation sulfuric acid and sugar liquid, sulfuric acid content 500mg/ml～700mg/ml, sugar liquid hold-up 60mg/ml～80mg/ml in maize straw acid hydrolysis solution; Specific as follows:
A, sequential simulated moving bed separation: described maize straw acid hydrolysis solution is separated by sequential type simulated moving bed chromatography equipment, sepn process one-period comprises 8 steps, each step comprises three phases, first stage is separation phase, 8 root chromatogram columns are connected in series, being extracted out by liquid in post by the recycle pump being arranged under the 3rd post and inject the 4th post, in the 4th post, liquid injects the 5th post, back and forth carries out cyclical operation successively; Subordinate phase is desorption phase, enters strippant on the 1st post top, releases sulphuric acid soln under the 6th post; Phase III is charging desorption phase, enters strippant on the 1st post top, and the 5th root chromatogram column top enters described maize straw acid hydrolysis solution, releases sugar soln, release sulphuric acid soln under the 6th root chromatogram column under the 1st post;After this three phases completes, the opening for feed of desorption phase and charging desorption phase and discharge port move a chromatographic column all successively backward, repeat the three phases of each step again, it one week is that one-period terminates that 8 steps complete i.e. 8 root chromatogram column rotation, next the next cycle is entered, method is identical with one-period, circulates successively, until sepn process reaches stable state; The sulphuric acid soln concentration that obtains of separation is 210mg/mL～320mg/mL, purity is 93%～98%, and sugar soln concentration is 20mg/mL～41mg/mL, purity 93%～96%;
B, sulphuric acid soln concentration and recovery: the sulphuric acid soln obtained through a step is carried out rotary evaporation process, temperature 50 DEG C～65 DEG C, obtains concentrated solution, and concentrated solution concentration is 500mg/mL～550mg/mL;
C, sugar soln filter: filtered by obtained for a step sugar soln micron-rated filter, the yellow liquid of obtained clarification;
D, sugar soln are concentrated: obtained for step c sugar soln is carried out rotary evaporation process, and temperature is 60～65 DEG C, the yellow liquid of obtained clarification.
2. the method for saccharic acid in sequential simulated moving bed separating corn stalk acid hydrolysis solution according to claim 1, it is characterised in that: the preparation method of described maize straw acid hydrolysis solution:
The preparation of the first step, maize straw acid hydrolysis solution: maize straw is dried, pulverized 40 order sieves, take 2g corn stalk powder, add the sulphuric acid soln 100mL of volumetric concentration 3%, it is placed in microwave extracting instrument, adjustment microwave power 700W, temperature 80 DEG C, reaction 153min, obtains maize straw acid hydrolysis solution;
2nd step, the maize straw acid hydrolysis solution filtration the first step obtained with filter paper, obtain clarification dark brown liquid, and utilizes Rotary Evaporators to be concentrated to solution sulfuric acid content 500mg/ml～700mg/ml, sugar liquid hold-up 60mg/ml～80mg/ml.
3. the method for saccharic acid in sequential simulated moving bed separating corn stalk acid hydrolysis solution according to claim 2, it is characterised in that: in described sequential simulated moving bed separation, sorbent material is Zeo-karb UBK08, IR120H+、IR118H+、IR120Na+Or AMBERJETC1H+In any one; Strippant is deionized water, and separation temperature is 50 DEG C～55 DEG C, and first stage internal circulating load is 410～550mL; Subordinate phase, strippant flow is 23～45mL/min, and desorption time is 110～160s; Phase III, strippant flow is 30～45mL/min, and charging amount is 35～50mL/min, charging and desorption time is 120～180s.
4. the method for saccharic acid in sequential simulated moving bed separating corn stalk acid hydrolysis solution according to claim 3, it is characterized in that: the sulphuric acid concentration liquid dilution that described step b obtains obtains the sulphuric acid soln of volumetric concentration 3%, is recycled and reused in the first step prepared by maize straw acid hydrolysis solution.
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