Office Action 1: Non-Final Rejection (2025-05-20)
Rejection types: 102 - Lack of Novelty, 112 - Written Description/Enablement

CLAIMS:
CLAIMS

1\. A process to perform a controlled exothermic delignification of biomass at a temperature below 500C.2. A process to perform a controlled exothermic delignification of biomass, said process comprising the steps of:
\- providing a system comprising at least a first vessel and a second vessel;
\- providing said biomass comprising lignin, hemicellulose and cellulose fibers into said first vessel;
\- providing an aqueous acidic composition comprising a sulfuric acid component;
\- providing a modifier component;
\- providing a peroxide component;
\- exposing said biomass to said sulfuric acid, modifier and peroxide components, creating a reaction mass;
\- mixing said reaction mass;
\- allowing said sulfuric acid, modifier and peroxide components to come into contact with said biomass for a period of time sufficient to a delignification reaction to occur and remove a pre- determined amount of said lignin from said biomass;
wherein said pre-determined amount is assessed by testing a first kappa number, with a suitable apparatus, of the biomass, when said first kappa number of said biomass is reached, the biomass is transferred to said second vessel;- allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel;
\- allowing said sulfuric acid component and peroxide component to continue said delignification reaction at said second temperature and remove a second pre-determined amount of said lignin from said biomass;wherein said second pre-determined amount is assessed by testing a second kappa number, with a suitable apparatus, of the biomass, when said second kappa number of said biomass is reached, the biomass is removed from said second vessel;- optionally, a washing step is employed to separate a resulting liquid portion comprising said lignin and hemicellulose from the solid portion containing the cellulose extracted from the biomass.

3\. The process according to claim 2, wherein said system comprises a third vessel where the biomass is sent to after being removed form said second vessel,
\- allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel;
\- allowing said sulfuric acid, modifier and peroxide components to continue said delignification reaction at said second temperature and remove a third pre-determined amount of said lignin from said biomass;
wherein said third pre-determined amount is assessed by testing a third kappa number, with a suitable apparatus, of the biomass, when said third kappa number of said biomass is reached, the biomass is removed from said third vessel.
4\. The process according to claim 3, where said process requires temperature control at said first vessel, said second vessel and said third vessel.
5\. The process according to claim 4, where said temperature control comprises a heat exchanger,
jacketed vessel and baffles
6\. The process according to any one of claims 4 or 5, where said primary temperature control is a heat exchanger, secondary control is a jacketed tank and tertiary control is a baffle
7\. The process according to any one of claims 1 to 6, where said system has an outlet which allows the separation of solids from liquids.
8\. The process according to any one of claims 1 to 7, where said mixing in said first vessel is performed by a recirculation of the reaction mass.
9\. The process according to any one of claims 1 to 8, where said mixing in said second vessel is performed by a paddle mixer.

10\. The process according to any one of claims 1 to 9, where said mixing in said third vessel is performed by a paddle mixer.

11\. The process according to any one of claims 1 to 10, where said sulfuric acid component comes from a modified Caro's acid composition selected from the group consisting of composition A; composition B and Composition C;

wherein said composition A comprises:- sulfuric acid in an amount ranging from 20 to 70 wt% of the total weight of the composition;
\- a modifier component comprising an amine moiety and a sulfonic acid moiety selected from the group consisting of: taurine; taurine derivatives;
and taurine-related compounds; and
\- a peroxide;
wherein said composition B comprises:- an alkylsulfonic acid; and
\- a peroxide; wherein the acid is present in an amount ranging from 40 to 80 wt% of the total weight of the composition and where the peroxide is present in an amount ranging from 10 to 40 wt% of the total weight of the composition;
wherein said composition C comprises:- sulfuric acid;
\- a two-part modifier component comprising:
\- a compound comprising an amine moiety; and
\- a compound comprising a sulfonic acid moiety; and
\- a peroxide.

12\. The process according to any one of claims 1 to 10, where the temperature of the reaction mass is maintained at a temperature ranging from 30 - 45°C.

13\. The process according to any one of claims 1 to 12, wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to treat at least one additional biomass batch.

14\. The process according to any one of claims 1 to 12, wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to treat at least four additional biomass batches.

15\. The process according to any one of claims 1 to 12, wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to further treat additional biomass batches until the peroxide concentration reaches less than 1%.

OFFICE ACTION:
Detailed Office Action
The communication dated 8/10/2023 has been entered and fully considered.
Claims 1-15 are pending.
Notice of Pre-AIA  or AIA  Status
The present application, filed on or after March 16, 2013, is being examined under the first inventor to file provisions of the AIA .
Drawings
The drawings are objected to as failing to comply with 37 CFR 1.84(p)(5) because they include the following reference character(s) not mentioned in the description:
Figure 1: 114, 122, 132, 142, and 144.
Figure 2: 212, 222, 227, 232, 237, 242, 246, 248
Drawing sheets in compliance with 37 CFR 1.121(d), or amendment to the specification to add the reference character(s) in the description in compliance with 37 CFR 1.121(b) are required in reply to the Office action to avoid abandonment of the application. Any amended replacement drawing sheet should include all of the figures appearing on the immediate prior version of the sheet, even if only one figure is being amended. Each drawing sheet submitted after the filing date of an application must be labeled in the top margin as either “Replacement Sheet” or “New Sheet” pursuant to 37 CFR 1.121(d). If the changes are not accepted by the examiner, the applicant will be notified and informed of any required corrective action in the next Office action. The objection to the drawings will not be held in abeyance.
The drawings are objected to as failing to comply with 37 CFR 1.84(p)(5) because they do not include the following reference sign(s) mentioned in the description: 201 and 202.  Corrected drawing sheets in compliance with 37 CFR 1.121(d) are required in reply to the Office action to avoid abandonment of the application. Any amended replacement drawing sheet should include all of the figures appearing on the immediate prior version of the sheet, even if only one figure is being amended. Each drawing sheet submitted after the filing date of an application must be labeled in the top margin as either “Replacement Sheet” or “New Sheet” pursuant to 37 CFR 1.121(d). If the changes are not accepted by the examiner, the applicant will be notified and informed of any required corrective action in the next Office action. The objection to the drawings will not be held in abeyance.
Allowable Subject Matter
Claim 2 would be allowable if rewritten or amended to overcome the rejection(s) under 35 U.S.C. 112(b) or 35 U.S.C. 112 (pre-AIA ), 2nd paragraph, set forth in this Office action.
Claim Rejections - 35 USC § 112
The following is a quotation of 35 U.S.C. 112(b):
(b)  CONCLUSION.—The specification shall conclude with one or more claims particularly pointing out and distinctly claiming the subject matter which the inventor or a joint inventor regards as the invention.
The following is a quotation of 35 U.S.C. 112 (pre-AIA ), second paragraph:
The specification shall conclude with one or more claims particularly pointing out and distinctly claiming the subject matter which the applicant regards as his invention.
Claims 2-15 are rejected under 35 U.S.C. 112(b) or 35 U.S.C. 112 (pre-AIA ), second paragraph, as being indefinite for failing to particularly point out and distinctly claim the subject matter which the inventor or a joint inventor (or for applications subject to pre-AIA  35 U.S.C. 112, the applicant), regards as the invention.
In claim 2 line 24 the applicant claims “a suitable apparatus” for measuring “the second kappa number”.  It is not clear if this should be “the suitable apparatus” used to measure “the first kappa number” or “a second suitable apparatus”.  That is, is the same apparatus used or different apparatuses used.  Figure 1 appears to show that different apparatuses are used.
Claim 2 recites the limitation said second temperature in lines 20-21.  There is insufficient antecedent basis for this limitation in the claim.
In claim 2 the applicant mixes the biomass with chemicals in the first reactor.  This forms a first treated biomass.  However, later in the claim the applicant refers to the treated biomass in the second reactor as “said biomass”.  Therefore the applicant is using the same term to refer to two different biomass.  The Examiner suggests the applicant states that the first reactor forms “a first treated biomass” and then use that term later in the claim.
Similarly the applicant claims a washing step on the biomass.  The applicant should claim that the second reactor forms “a second treated biomass” and that “the second treated biomass” is washed.
Claims 3-15 depend from claim 2 and are similarly rejected.
In claim 3, the applicant refers to the treated biomass in the second reactor as “said biomass” however this is not the same biomass as defined earlier in claim 1 but has undergone a treatment in the first vessel and second vessel.
In claim 3 the applicant claims “a suitable apparatus” for measuring “said third kappa number”.  It is not clear if this should be “the suitable apparatus” used to measure “the first kappa number” or “a third suitable apparatus”.  That is, is the same apparatus used or different apparatuses used.  Figure 1 appears to show that different apparatuses are used.
Claim 6 recites the limitation said primary temperature control in line 2.  There is insufficient antecedent basis for this limitation in the claim.
Claims 9 and 10 recite the limitation said mixing in line 2.  There is insufficient antecedent basis for this limitation in the claim. The parent claims 2 and 3 do not state that mixing occurs in the second vessel or the third vessel.
Claim 10 should depend upon claim 3 as the third vessel is not mentioned until claim 3.
Claim 11 uses 3 specific compositions and states that the sulfuric acid comes from a modified Caro’s acid of 3 different compositions.  Each of the compositions mentions a modifier and a peroxide.  It is not clear if these modifiers and peroxides are in addition to the modifies and peroxide of claim 2.  As written, it appears the claim requires two modifiers because composition A/B/C is the sulfuric acid of claim 2.
In claim 12 it is not clear if this refers to the reaction mass in the first reactor or second reactor or both.
Claims 13-15 recite the limitation the reaction in line 2.  There is insufficient antecedent basis for this limitation in the claim.
Claim Rejections - 35 USC § 102
The following is a quotation of the appropriate paragraphs of 35 U.S.C. 102 that form the basis for the rejections under this section made in this Office action:
A person shall be entitled to a patent unless –
(a)(1) the claimed invention was patented, described in a printed publication, or in public use, on sale, or otherwise available to the public before the effective filing date of the claimed invention.
Claim 1 is rejected under 35 U.S.C. 102(a)(1) as being clearly anticipated by WO 98/02612 AKHTAR et al., hereinafter AKHTAR.
AKHTAR discloses treating wood chips with a fungus at controlled temperature of 27-35 degrees C which falls within the claimed range [abstract, claims 1 and 3].  AKHTAR discloses that white rot fungus delignification is exothermic [pg. 5 lines 9-15].
Conclusion


NEXT OFFICE ACTION: EXAMINER'S AMENDMENT
An examiner’s amendment to the record appears below. Should the changes and/or additions be unacceptable to applicant, an amendment may be filed as provided by 37 CFR 1.312. To ensure consideration of such an amendment, it MUST be submitted no later than the payment of the issue fee.
Authorization for this examiner’s amendment was given in an interview with Attorney Brent Johnson on 10/7/2025.
The application has been amended as follows:
Claim 2 has been replaced by the following:
A process to perform a controlled exothermic delignification of biomass, said process comprising the steps of:
- providing a system comprising at least a first vessel and a second vessel;
- providing biomass comprising lignin, hemicellulose and cellulose fibers into said first vessel;
- providing an aqueous acidic composition comprising a sulfuric acid component;
- providing a modifier component;
- providing a peroxide component;
- exposing said biomass to said sulfuric acid component, modifier and peroxide components, creating a reaction mass;
- mixing said reaction mass;
- allowing said sulfuric acid, modifier and peroxide components to come into contact with said reaction mass for a period of time sufficient to a delignification reaction to occur and remove a pre-determined amount of said lignin from said reaction mass;
wherein said pre-determined amount is assessed by testing a first kappa number, with a first suitable apparatus, of the reaction mass when said first kappa number of said reaction mass is reached a first treated biomass is formed, the first treated biomass is transferred to said second vessel;
- allowing the temperature of the first treated biomass to increase during the residence time of said first treated biomass in said second vessel;
- allowing said sulfuric acid component and peroxide component to continue said delignification reaction at a second temperature and remove a second pre-determined amount of said lignin from said first treated biomass;
wherein said second pre-determined amount is assessed by testing a second kappa number, with a second suitable apparatus, of the first treated biomass, when said second kappa number of said first treated biomass is reached a second treated biomass is formed, the second treated biomass is then removed from said second vessel;
- optionally, a washing step is employed to separate a resulting liquid portion comprising said lignin and hemicellulose from a solid portion containing the cellulose extracted from the second treated biomass, said washing step thereby forming a washed biomass.
---
Claim 3 has been replaced by the following:
The process according to claim 2, wherein said system comprises a third vessel where the second treated biomass is sent to after being removed form said second vessel,
- allowing the temperature of the second treated biomass to increase during the residence time of said second treated biomass in said third vessel;
- allowing said sulfuric acid, modifier and peroxide components to continue said
delignification reaction at said third temperature and remove a third pre-
determined amount of said lignin from said second treated biomass;
wherein said third pre-determined amount is assessed by testing a third kappa number, with a third suitable apparatus, of the second treated biomass, when said third kappa number of said second treated biomass is reached a third treated biomass is formed, the third treated biomass is removed from said third vessel.
--
Claim 12 has been replaced by the following:
The process according to claim 4, where the temperature of said first vessel or said second vessel is maintained at a temperature ranging from 30-45°C.
--
In claim 13 line 2 after the word “liquid” the word “portion” has been added.
In claim 14 line 2 after the word “liquid” the word “portion” has been added.
In claim 15 line 2 after the word “liquid” the word “portion” has been added.
Reasons for Allowance
The following is an examiner’s statement of reasons for allowance:  It is known to bleach pulp (delignified biomass) with sulfuric acid, peroxide, and modifiers.  The prior art did not suggest treating a biomass in a multi-stage system with peroxide, sulfuric acid, and a modifier and pulping to a first kappa number in the first stage and pulping to a second kappa number in the second stage.
Any comments considered necessary by applicant must be submitted no later than the payment of the issue fee and, to avoid processing delays, should preferably accompany the issue fee.  Such submissions should be clearly labeled “Comments on Statement of Reasons for Allowance.”
Conclusion

CITED REFERENCE SUMMARIES: Ref US9394648B2: Claims:
A method for treating wood chips, the method comprising the steps of: (i) exposing a first mixture comprising the wood chips and an aqueous sulfuric acid solution, between about 1.0 and about 1.5% (w/w), at a temperature of between about 150Â° C. and about 180Â° C. for a period of time between about 15 and about 30 minutes, wherein the mixture has a consistency of between about 10 and about 25%, to at least partially hydrolyze hemicellulose of the wood chips; (ii) removing xylose and mannose produced in step (i) from the mixture; (iii) exposing a second mixture comprising the wood chips produced in step (i) and an aqueous sulfuric acid solution, between about 3.0 and about 10% (w/w), at a temperature of between about 180Â° C. and about 220Â° C., wherein the second mixture has a consistency of between about 10 and about 25%, to at least partially hydrolyze hemicellulose of the wood chips; and (iv) physically reducing the wood chips produced in step (iii) by disc refining to produce cellulosic fibers which will undergo hydrolysis to produce glucose at a yield of at least 90% in presence of a cellulase dosage of 15 FPU/g glucan, and wherein net specific energy consumed in step (iv) is reduced by between 70 and 95 percent when compared to disc refining of the same amount of wood chips not subjected to acid treatment under the same disc refining conditions of step (iv).
(i) exposing a first mixture comprising the wood chips and an aqueous sulfuric acid solution, between about 1.0 and about 1.5% (w/w), at a temperature of between about 150Â° C. and about 180Â° C. for a period of time between about 15 and about 30 minutes, wherein the mixture has a consistency of between about 10 and about 25%, to at least partially hydrolyze hemicellulose of the wood chips;
(ii) removing xylose and mannose produced in step (i) from the mixture;
(iii) exposing a second mixture comprising the wood chips produced in step (i) and an aqueous sulfuric acid solution, between about 3.0 and about 10% (w/w), at a temperature of between about 180Â° C. and about 220Â° C., wherein the second mixture has a consistency of between about 10 and about 25%, to at least partially hydrolyze hemicellulose of the wood chips; and
(iv) physically reducing the wood chips produced in step (iii) by disc refining to produce cellulosic fibers which will undergo hydrolysis to produce glucose at a yield of at least 90% in presence of a cellulase dosage of 15 FPU/g glucan, and wherein net specific energy consumed in step (iv) is reduced by between 70 and 95 percent when compared to disc refining of the same amount of wood chips not subjected to acid treatment under the same disc refining conditions of step (iv).
Ref US20250052002A1: Claims:
A process to perform a controlled exothermic delignification on a batch of lignocellulosic biomass, said process comprising: providing a system comprising at least a first vessel and a second vessel; providing said biomass comprising lignin, hemicellulose and cellulose fibers into said first vessel; providing an aqueous acidic composition comprising an acid selected from the group consisting of: sulfuric acid; an alkylsulfonic acid; an arylsulfonic acid and combinations thereof; providing a modifier component; providing a peroxide component; exposing said biomass to said said acidic composition, said peroxide component and said modifier component to create a reaction mass; mixing said reaction mass; allowing said said acidic composition and peroxide component to come into contact with said biomass for a period of time sufficient to a delignification reaction to occur and remove a pre-determined amount of said lignin from said biomass, wherein said pre-determined amount is assessed by determining a first remaining peroxide concentration in the reaction mass, with a suitable apparatus, when said first remaining peroxide concentration is reached, the biomass is transferred to said second vessel; allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel; allowing said acidic composition, said modifier component and said peroxide component to continue said delignification reaction at said second temperature and remove a second pre-determined amount of said lignin from said biomass, wherein said second pre-determined amount is assessed by testing a second remaining peroxide concentration, with a suitable apparatus, in the reaction mass, when said second remaining peroxide concentration is reached, the biomass is removed from said second vessel; and optionally, a washing step is employed to separate a resulting liquid portion comprising said lignin and hemicellulose from the solid portion containing the cellulose extracted from the biomass.
providing a system comprising at least a first vessel and a second vessel;
providing said biomass comprising lignin, hemicellulose and cellulose fibers into said first vessel;
providing an aqueous acidic composition comprising an acid selected from the group consisting of: sulfuric acid; an alkylsulfonic acid; an arylsulfonic acid and combinations thereof;
providing a modifier component;
providing a peroxide component;
exposing said biomass to said said acidic composition, said peroxide component and said modifier component to create a reaction mass;
mixing said reaction mass;
allowing said said acidic composition and peroxide component to come into contact with said biomass for a period of time sufficient to a delignification reaction to occur and remove a pre-determined amount of said lignin from said biomass, wherein said pre-determined amount is assessed by determining a first remaining peroxide concentration in the reaction mass, with a suitable apparatus, when said first remaining peroxide concentration is reached, the biomass is transferred to said second vessel;
allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel;
allowing said acidic composition, said modifier component and said peroxide component to continue said delignification reaction at said second temperature and remove a second pre-determined amount of said lignin from said biomass, wherein said second pre-determined amount is assessed by testing a second remaining peroxide concentration, with a suitable apparatus, in the reaction mass, when said second remaining peroxide concentration is reached, the biomass is removed from said second vessel; and
optionally, a washing step is employed to separate a resulting liquid portion comprising said lignin and hemicellulose from the solid portion containing the cellulose extracted from the biomass.
The process according to claim 1 , wherein said system comprises a third vessel where the biomass is sent to after being removed form said second vessel, and further comprising: allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel; and allowing said acidic composition, said modifier component and said peroxide component to continue said delignification reaction at said second temperature and remove a third pre-determined amount of said lignin from said biomass, wherein said third pre-determined amount is assessed by testing a third remaining peroxide concentration, with a suitable apparatus, in the reaction mass, when said third remaining peroxide concentration in said reaction mass is reached, the biomass and the aqueous acid composition are removed from said third vessel.
allowing the temperature of the biomass mixture to increase during the residence time of said biomass in said second vessel; and
allowing said acidic composition, said modifier component and said peroxide component to continue said delignification reaction at said second temperature and remove a third pre-determined amount of said lignin from said biomass, wherein said third pre-determined amount is assessed by testing a third remaining peroxide concentration, with a suitable apparatus, in the reaction mass, when said third remaining peroxide concentration in said reaction mass is reached, the biomass and the aqueous acid composition are removed from said third vessel.
The process according to claim 2 , where said process requires temperature control at said first vessel, and said second vessel.
The process according to claim 3 , where said temperature control comprises a heat exchanger, jacketed vessel and baffles.
The process according to claim 4 , where said primary temperature control is a heat exchanger, secondary control is a jacketed tank and tertiary control is a baffle.
The process according to claim 5 , where said system has an outlet which allows the separation of solids from liquids.
The process according to claim 6 , where said mixing in said first vessel is performed by a recirculation of the reaction mass.
The process according to claim 7 , where said mixing in said second vessel is performed by a paddle mixer.
The process according to claim 8 , where said mixing in said third vessel is performed by a paddle mixer.
The process according to claim 1 , where said said acidic composition, said modifier component and said peroxide component form a modified Caro's acid composition selected from the group consisting of composition A; composition B and Composition C; wherein said composition A comprises: sulfuric acid in an amount ranging from 20 to 70 wt % of the total weight of the composition; a modifier component comprising an amine moiety and a sulfonic acid moiety selected from the group consisting of taurine; taurine derivatives; and taurine-related compounds; and a peroxide; wherein said composition B comprises: an alkyl sulfonic acid; and a peroxide; wherein the acid is present in an amount ranging from 40 to 80 wt % of the total weight of the composition and where the peroxide is present in an amount ranging from 10 to 40 wt % of the total weight of the composition; wherein said composition C comprises: sulfuric acid; and a two-part modifier component comprising: a compound comprising an amine moiety; a compound comprising a sulfonic acid moiety; and a peroxide.
wherein said composition A comprises: sulfuric acid in an amount ranging from 20 to 70 wt % of the total weight of the composition; a modifier component comprising an amine moiety and a sulfonic acid moiety selected from the group consisting of taurine; taurine derivatives; and taurine-related compounds; and a peroxide;
sulfuric acid in an amount ranging from 20 to 70 wt % of the total weight of the composition;
a modifier component comprising an amine moiety and a sulfonic acid moiety selected from the group consisting of taurine; taurine derivatives; and taurine-related compounds; and
wherein said composition B comprises: an alkyl sulfonic acid; and a peroxide; wherein the acid is present in an amount ranging from 40 to 80 wt % of the total weight of the composition and where the peroxide is present in an amount ranging from 10 to 40 wt % of the total weight of the composition;
an alkyl sulfonic acid; and
a peroxide; wherein the acid is present in an amount ranging from 40 to 80 wt % of the total weight of the composition and where the peroxide is present in an amount ranging from 10 to 40 wt % of the total weight of the composition;
wherein said composition C comprises: sulfuric acid; and a two-part modifier component comprising: a compound comprising an amine moiety; a compound comprising a sulfonic acid moiety; and a peroxide.
sulfuric acid; and
a two-part modifier component comprising: a compound comprising an amine moiety; a compound comprising a sulfonic acid moiety; and a peroxide.
a compound comprising an amine moiety;
a compound comprising a sulfonic acid moiety; and
The process according to claim 1 , where the temperature of the reaction mass is maintained at a temperature ranging from 25-45Â° C.
The process according to claim 1 , wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to treat at least one additional biomass batch.
The process according to claim 1 , wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to treat at least four additional biomass batches.
The process according claim 1 , wherein at least part of the resulting liquid portion obtained at the end of the reaction is used to further treat additional biomass batches until the peroxide concentration reaches less than 1%.
A continuous digester adapted for use in the delignification of lignocellulosic biomass with a modified Caro's acid composition, where said continuous digester comprises: a cylindrical vessel comprising a first extremity and a second extremity; a diameter to length ratio of said vessel ranging from 0.08-0.2; a biomass wt % loading ranging from 3-15% relative to delignification blend in the digester; a gauge pressure to be 0-14 psi and a temperature to remain below 60Â° C.; an inlet, located at said first extremity, for loading said digester with said biomass component and said modified Caro's acid thus creating a reaction mixture; at least two zones for mixing a reaction mixture comprising said modified Caro's acid and said biomass component, said at least two zones being positioned sequentially within said cylindrical vessel, and each one of said at least two zones comprising: a temperature indicator/controller to monitor changes in a pre-determined temperature set point, to control heat exchanger setpoint, jet nozzles flow; a jet nozzle, located at a top section of said zone, to provide pumping mixing of the reaction mixture comprising said biomass component and said modified Caro's acid; an extraction screen, located proximate at a bottom section of said zone, to allow the extraction of said modified Caro's acid from the bottom section of said zone; a screen section on the vertical plane having perforations of a shape selected from the group consisting of: circle, rectangular, square etc. and where screen size openings ranging from ââ³ to 6â³; a piping connected to said extraction screen and said jet nozzle to allow for recirculation of said modified Caro's acid from the bottom section of the zone to said top section of said zone; a chiller and heater feed loop, located outside of said zone, to allow for chilling/heating the modified Caro's acid solution to desired parameters; a Kappa number analyzer to allow the determination of the pulping percentage of the biomass; and a peroxide analyzer to allow the determination of the peroxide consumption; and a cone bottom adapted with an outlet, located at said second extremity, for discharging of the reaction mass.
a cylindrical vessel comprising a first extremity and a second extremity;
a diameter to length ratio of said vessel ranging from 0.08-0.2;
a biomass wt % loading ranging from 3-15% relative to delignification blend in the digester;
a gauge pressure to be 0-14 psi and a temperature to remain below 60Â° C.;
an inlet, located at said first extremity, for loading said digester with said biomass component and said modified Caro's acid thus creating a reaction mixture;
at least two zones for mixing a reaction mixture comprising said modified Caro's acid and said biomass component, said at least two zones being positioned sequentially within said cylindrical vessel, and each one of said at least two zones comprising: a temperature indicator/controller to monitor changes in a pre-determined temperature set point, to control heat exchanger setpoint, jet nozzles flow; a jet nozzle, located at a top section of said zone, to provide pumping mixing of the reaction mixture comprising said biomass component and said modified Caro's acid; an extraction screen, located proximate at a bottom section of said zone, to allow the extraction of said modified Caro's acid from the bottom section of said zone; a screen section on the vertical plane having perforations of a shape selected from the group consisting of: circle, rectangular, square etc. and where screen size openings ranging from ââ³ to 6â³; a piping connected to said extraction screen and said jet nozzle to allow for recirculation of said modified Caro's acid from the bottom section of the zone to said top section of said zone; a chiller and heater feed loop, located outside of said zone, to allow for chilling/heating the modified Caro's acid solution to desired parameters; a Kappa number analyzer to allow the determination of the pulping percentage of the biomass; and a peroxide analyzer to allow the determination of the peroxide consumption; and
a temperature indicator/controller to monitor changes in a pre-determined temperature set point, to control heat exchanger setpoint, jet nozzles flow;
a jet nozzle, located at a top section of said zone, to provide pumping mixing of the reaction mixture comprising said biomass component and said modified Caro's acid;
an extraction screen, located proximate at a bottom section of said zone, to allow the extraction of said modified Caro's acid from the bottom section of said zone;
a screen section on the vertical plane having perforations of a shape selected from the group consisting of: circle, rectangular, square etc. and where screen size openings ranging from ââ³ to 6â³;
a piping connected to said extraction screen and said jet nozzle to allow for recirculation of said modified Caro's acid from the bottom section of the zone to said top section of said zone;
a chiller and heater feed loop, located outside of said zone, to allow for chilling/heating the modified Caro's acid solution to desired parameters;
a Kappa number analyzer to allow the determination of the pulping percentage of the biomass; and
a peroxide analyzer to allow the determination of the peroxide consumption; and
a cone bottom adapted with an outlet, located at said second extremity, for discharging of the reaction mass.
The continuous digester according to claim 15 , wherein said digester is positioned vertically with the inlet being located a top portion thereof and the outlet located at a bottom portion of said digester.
Ref US12195919B2: Claims:
A method for preparing agricultural materials as a feedstock for use as a pulp, the method comprising: providing non-wood agricultural feedstock that includes agricultural fibers; shredding, wetting, and conditioning the non-wood agricultural feedstock in a preliminary alkaline low consistency pulping module at a low consistency of from 1% to 10% at a low temperature to produce partially pulped agricultural fibers, such step including separating some lignin and hemicellulose from the partially pulped agricultural fibers; introducing the partially pulped agricultural fibers into a first reactor, wherein the first reactor operates at a low temperature of less than 100° C.; removing at least a portion of black liquor generated in the first reactor with a portion of the black liquor being recirculated to the preliminary alkaline low consistency pulping module, and a remainder being sent for recovery of hemicellulose and/or lignin therein; and introducing the partially pulped agricultural fibers from the first reactor into a second reactor, where the second reactor operates at a low temperature, of less than 100° C., the second reactor operating at a higher temperature than the first reactor, to produce pulped agricultural fibers; wherein the preliminary alkaline low consistency pulping module operates at a temperature in a range of 40° C. to less than 100° C., and the preliminary alkaline low consistency pulping module has a residence time of less than 30 minutes.
providing non-wood agricultural feedstock that includes agricultural fibers;
shredding, wetting, and conditioning the non-wood agricultural feedstock in a preliminary alkaline low consistency pulping module at a low consistency of from 1% to 10% at a low temperature to produce partially pulped agricultural fibers, such step
[Truncated to input limit]