Hydrolysis Reactor Research Articles

Process simulation of cassava cellulosic ethanol production with low to medium-pressure steam heat integration

Energy demand tends to increase by 80% in 2050 due to the rapid growth of the global population. However, the energy resources rapidly decrease for responding to the global need. Many previous researchers suggest the ideas for solving this situation and the most interesting solution is the heat integration which intends to produce cost-effective energy with minimal impact on the environment. Energy integration thus should be noticeable for the industry process to minimize the loss along the industrial process. The ethanol production process is interested in this study because it can add value to agricultural products like cassava which is an industrial crop in several countries and produces ethanol products that can decrease the usage of gasoline. Here, the heat integration model was developed for the ethanol production process by using low to medium-pressure steam. For the simulation model, the ethanol production process used the cellulose content as the main inlet component to be easy for applicable corresponding to feed casava cellulosic substances. The process contained three sections including enzymatic hydrolysis, simultaneous saccharification fermentation (SSF), and fractional distillation. The quality and quantity of low to medium-pressure steam were investigated for maintaining the operation of the enzymatic hydrolysis reactor by varying steam pressure between 1–2 atm and steam temperature between 100–105 °C. The results achieved the methodology to find optimum conditions by the ratio between steam flow rate and product quantity. The best case could reduce 6.49% of the excessive usage of low to medium-pressure steam which pointed out the way to use the energy efficiently.

Geometric Optimization of Hydrolysis Reactors to Enhance MgH2 Hydrolysis Performance

Geometric Optimization of Hydrolysis Reactors to Enhance MgH₂ Hydrolysis Performance

The Material Flow and Stability Performance of the Anaerobic Digestion of Pig Manure after (Hyper)-Thermophilic Hydrolysis Is Introduced: A Comparison with a Single-Stage Process

Slow hydrolysis persistently affects the anaerobic digestion of animal manure. Thermophilic and hyper-thermophilic treatments introduced into a two-stage anaerobic process treating pig manure were investigated, with a single-stage mesophilic process as a control. The results from the 100-day experiment showed the thermophilic-mesophilic system had the highest removal efficiency of volatile solids at 60.8%, 18% higher than the single-stage process. The thermophilic and hyper-thermophilic hydrolysis reactors contributed 23.5% and 21.7% solubilization of chemical oxygen demand (COD), respectively. The hydrolysis efficiency achieved in the single process was 49.7%, which was lower than the hydrolysis in the two-stage processes. Approximately 60% of COD was distributed in the solid fraction in the first stage, and more than half of the particle COD continued to hydrolyze in the subsequent second stage. The mass balance of COD and volatile solids removal performance illustrated the advantages of the temperature-phased process. Comparatively, the three mesophilic reactors all had strong stability.

Continuous-flow synthesis of amphiphilic rhodamine B-polymethylsilsesquioxane fluorescent microspheres for micro-PIV analysis

• Rhodamine B- polymethylsilsesquioxane fluorescent microspheres were prepared. • Synthetic process was performed in a one-step continuous-flow microreaction system. • The hydrophilic and hydrophobic RhB-PMSQ microspheres were synthesized. • Amphiphilic RhB-PMSQ particles were used as tracer particles for micro-PIV analysis. Tracer particle is a key element in the micro-PIV flow field measurements. The oil-dispersible tracer particles are mainly obtained by post modification, resulting in relatively poor uniformity and dispersibility. In this work, we developed a molecular-level amphiphilic tracer particle, i.e., rhodamine B-polymethylsilsesquioxane (RhB-PMSQ) fluorescent microspheres. The RhB-PMSQ microspheres were synthesized in a continuous-flow microreaction system with the aqueous solution of NH 4 OH and RhB as the continuous phase and methyltrimethoxysilane (MTMS) as the dispersed phase. The microreaction system consisted of a T -junction micromixer, a capillary reactor for MTMS hydrolysis, and a millimeter-scale tubular reactor for condensation reaction. By controlling the condensation degree of surface Si-OH groups, the hydrophilic and hydrophobic RhB-PMSQ microspheres could be synthesized with the same reaction system, and they could be uniformly dispersed in the aqueous phase and oil phase, respectively. The density, pore structure, and fluorescence property of the RhB-PMSQ microspheres were investigated in detail. The RhB-PMSQ microspheres were employed as the tracer particles of water and liquid paraffin, and the two-phase velocity profiles were measured via micro-PIV technique in a step T -junction microchannel. The micro-PIV results indicated that amphiphilic RhB-PMSQ microspheres could serve as the tracer particles for the flow field measurement both of aqueous phase and oil phase.

Two-stage anaerobic membrane bioreactor for co-treatment of food waste and kitchen wastewater for biogas production and nutrients recovery

Co-digestion of organic waste and wastewater is receiving increased attention as a plausible waste management approach toward energy recovery. However, traditional anaerobic processes for co-digestion are particularly susceptible to severe organic loading rates (OLRs) under long-term treatment. To enhance technological feasibility, this work presented a two-stage Anaerobic Membrane Bioreactor (2 S-AnMBR) composed of a hydrolysis reactor (HR) followed by an anaerobic membrane bioreactor (AnMBR) for long-term co-digestion of food waste and kitchen wastewater. The OLRs were expanded from 4.5, 5.6, and 6.9 kg COD m−3 d−1 to optimize biogas yield, nitrogen recovery, and membrane fouling at ambient temperatures of 25–32 °C. Results showed that specific methane production of UASB was 249 ± 7 L CH4 kg−1 CODremoved at the OLR of 6.9 kg TCOD m−3 d−1. Total Chemical Oxygen Demand (TCOD) loss by hydrolysis was 21.6% of the input TCOD load at the hydraulic retention time (HRT) of 2 days. However, low total volatile fatty acid concentrations were found in the AnMBR, indicating that a sufficiently high hydrolysis efficiency could be accomplished with a short HRT. Furthermore, using AnMBR structure consisting of an Upflow Anaerobic Sludge Blanket Reactor (UASB) followed by a side-stream ultrafiltration membrane alleviated cake membrane fouling. The wasted digestate from the AnMBR comprised 42–47% Total Kjeldahl Nitrogen (TKN) and 57–68% total phosphorous loading, making it suitable for use in soil amendments or fertilizers. Finally, the predominance of fine particles (D10 = 0.8 μm) in the ultrafiltration membrane housing (UFMH) could lead to a faster increase in trans-membrane pressure during the filtration process.

Oscillatory flow bioreactor operating at high solids loading for enzymatic hydrolysis of lignocellulosic biomass

Bioreactor technology applied to enzymatic hydrolysis has been studied to overcome the main limitation of enzymatic hydrolysis. This work presents the application of an oscillatory flow reactor (OFR) for enzymatic hydrolysis of lignocellulosic biomass at high solids loading [> 15% (w/v)]. OFR consists of a tubular reactor with periodical constrictions where vortices are created due to the oscillating flow determined by frequency and amplitude. This can be favorable for enzymatic hydrolysis as efficient mixtures can be accomplished at low shear rates. OFR batch operation was tested at 18% (w/v) to evaluate the amplitude (2 – 6 mm) and frequency (2 – 4 Hz) conditions that best fit the process using hydrothermally pretreated corncob and low enzyme dose. The conditions tested demonstrated a positive effect on the process, where at an amplitude of 6 mm and frequency of 4 Hz, an increment of 24–34% in productivity was observed. Then, three different fed-batch strategies were tested achieving 25% (w/v) solid loading where up to 170.0 g/L of glucose was obtained representing 97% saccharification yield. This novel contribution using OFR at high solids loading is crucial as advances in lignocellulosic biotransformation technology are still in demand to achieve efficient and economically feasible processes.

Process optimisation of controlled and continuous MgH2 hydrolysis to produce hydrogen

Hydrogen (H2) is an excellent energy carrier with advantages of high energy density, high combustibility, zero pollutant emissions, etc. Magnesium hydride (MgH2) is considered a good candidate for hydrogen storage because of its high hydrogen storage capacity. In this work, a hydrolysis reactor with a filter element was employed, enabling the MgH2 hydrolysis kinetics to improve and occur in a controllable and continuous manner. Specifically, the hydrolysis kinetics can be improved by adjusting the flow rate of the hydrolysis solution and adding additives such as graphite, aluminum sulfate, solid citric acid, etc. Optimising the equipment structure can reduce the MgH2 loss during the hydrolysis process. On this basis, using an improved filter element can achieve controllable and continuous MgH2 hydrolysis, resulting in stable hydrogen production for 12 h at a flow rate of 200–300 mL/min. The results obtained in this study provide a reference for the use of MgH2 to achieve controllable continuous hydrogen production in the field of fuel cells.

Geometric improvement of hydrolysis reactor structure to enhance the sustainable production of hydrogen from MgH2

Hydrogen is an important clean renewable energy carrier and has the advantages of high calorific value, low environmental impact, and wide availability. Magnesium hydride (MgH2) has attracted extensive attention due to its high hydrogen storage density; however, its poor hydrolysis kinetics limit its application. In this paper, the hydrolysis performance of MgH2 was studied in a self-made hydrolysis reactor, which included both a single tube structure and a plate tower structure. The hydrolysis reactor with the plate tower structure was conducive to achieving controllable and continuous MgH2 hydrolysis. Specifically, the plate tower structure can effectively strengthen the distribution of MgH2 materials, improve the liquid–solid mass transfer and reduce the surface coating. The results of this paper can expand the application of traditional reactors and provide a novel approach for the design of hydrolysis reactors for controllable continuous MgH2 hydrolysis.

A novel fluidized bed suitable for the hydrolysis step in CuCl hydrogen production cycle

In this paper, a novel design for a hydrolysis reactor step in the Cu–Cl thermochemical hydrogen production cycle is presented and investigated.The core concept of this hydrolysis reactor is recirculation of reaction steam, hence the name “Recirculating Steam Fluidized Bed” (RSFB). This design recirculates steam through the fluidized bed allowing for the unused steam to be consumed by the reaction. This design was found to reduce the total thermal energy requirement of the hydrolysis step by 50% while maintaining favorable reaction kinetics. The recirculating steam has the added benefit of increasing the concentration of product HCl, allowing for a more productive integration with downstream processes. Given the results presented here, it is suggested that the RSFB reactor be considered for adoption in the Cu–Cl cycle scale-up efforts.

Investigation of sludge dewatering efficiency in the thermal-hydrolysis reactor at various physical operational factors: Performance and fluid dynamic analysis

The sludge produced from various wastewater treatment is waste with various contaminants concentrated. A few decades ago, the sludge was contolled through direct discharge to the water phase, but further treatment is required due to additional environmental pollution issues. However, there are various available carbon-based resources in the sludge. The thermal hydrolysis process can reduce the discharged sludge quantity by improving the dewatering ability. The purpose of this study is to investigate the effect of the physical change factors of the thermal hydrolysis reactor (sludge amount, slope degree, stirring speed and residual oxygen quantity) on the dewatering capacity and solubilization of the thermal hydrolysis process. The highest dewatering capacity and efficiency showed when 7 kg of sludge was injected and slope control mode. The stir speed showed the best results at 150 rpm, but the increase in efficiency slowly up from 100 rpm. In addition, through CFD analysis, the high efficiency reactor slope was optimized. By investigating the performance of the thermal hydrolysis process under various physical conditions and the physical and chemical changes of final products, it is expected that it will be possible to suggest a way to vary the utilization according to the various characteristics of the sludge. Since the optimization of physical changes does not require additional economic cost input, it has the potential to secure the economic feasibility of sludge reduction technology.

A bio-inspired flexible squeezing reactor for efficient enzymatic hydrolysis of lignocellulosic biomass for bioenergy production

Wheat straw is a promising source that can be used to obtain clean energy through its bioconversion into biofuel. Enzymatic hydrolysis is considered as a key step in biofuel production. However, the poor mixing of enzymes and lignocellulosic substrates caused by the high viscosity of biomass slurry significantly astricts such a process. In this study, a novel bio-inspired flexible tube reactor was developed for enhancing mass transfer through squeezing at different parts to imitate the intestinal peristalsis. The results of the visualization experiment showed that the apparent vertical diffusion velocity at different position were about 1.4–4.2 times faster than the control without squeezing, when the concentration of model solution (carboxymethyl cellulose solution) was 5 g/L. More importantly, the apparent vertical diffusion velocity increased by 5.2 times as the concentration of model solution increased to 20 g/L at squeezing mode. When the total solid (TS) concentration of lignocellulosic slurry was increased to 7.5%, the bionic reactor showed an excellent performance on the enzymatic hydrolysis of wheat straw. The highest reducing sugar yield achieved 20.2 g/L with 71.8% of carbohydrate conversion after 170 min at 40 rpm, which was 2.1 times higher than the control without squeezing.

A hydrogen generator coupled to a hydrogen heater for small scale portable applications

This study aims to build and test a small scale portable device able to couple a hydrogen generation system (based on a NaBH4 solution as liquid H2 carrier) to a hydrogen heater (based on the exothermic catalytic combustion of the released H2). The hydrogen generating system is based on the hydrolysis of stabilized solutions of NaBH4 (fuel solutions) which are pumped into the hydrolysis reactor. The generated H2 feeds the catalytic combustor. Two catalysts have been developed for the H2 generation and the combustion reactions able to operate at room temperature without need of additional energy supply. For the NaBH4 hydrolysis a Co-B catalyst was supported on a perforated and surface treated stainless steel (SS316) home-made monolith. For the flameless H2 catalytic combustion a Pt catalyst was prepared on a commercial SiC foam. The device was automatized and tested for the on-demand production of heat at temperatures up to 100ºC. In steady state conditions the NaBH4 solution flow is controlling the H2 flux and therefore the heater temperature. Once the steady-state is reached the system responds in a few minutes to up and down temperature demands from 80 to 100 ºC. The catalysts have shown no deactivation during the tests carried out in several days.

Design and control of novel reaction–separation–recycle processes for the production of 4-hydroxybutyl acrylate

Two chemistry routes are known for 4-hydroxybutyl acrylate production: the direct esterification of acrylic acid with 1,4-butanediol, and the transesterification of methyl acrylate with 1,4-butanediol. However, very scarce information in the literature is available about industrial production, or design and operation of production processes. In this study, we propose three novel reaction–separation–recycle processes for 4-hydroxybutyl acrylate production by direct esterification based on solid catalyst. Use of solid catalysts may avoid well-known issues of the liquid catalysts like recovery and re-use of the catalyst, difficult product recovery, and corrosion. Due to the nature of the chemical system and reactions conditions, the chemistry is not 100% selective towards the acrylate, important amounts of diacrylate by-product being formed. All processes use fixed-bed tubular reactors to perform the reactions and distillation-based equipment to achieve the required separations. While all processes have a similar separation sequence, each has its key particularities: the RSR-A process accepts the loss of reactants due to formation and elimination from the process of the diacrylate, RSR-B converts the diacrylate into its reactants in the esterification reactor, while RSR-C converts the diacrylate in a dedicated hydrolysis reactor. A key element in the separation sequence is the use of pressure-swing distillation to make the difficult split of the alcohol/acrylate/diacrylate ternary mixture. All processes are capital and energy intensive. The economic analysis shows that the RSR-A process has the most favorable economics: a total annualized cost of 2 million $/y and a specific annualized cost of 100 $/t of product. A control structure for the RSR-C process is presented, the dynamic simulations showing its efficiency in rejecting various disturbances.

Effectiveness of oyster shell as alkali additive for two-stage anaerobic co-digestion: Carbon flow analysis

The objective of this study was to investigate the carbon flow of two-stage anaerobic co-digestion of kitchen waste, agricultural waste, and horse dung using oyster shells as pH control conditioners compared with using alkalis. The anaerobic system consisted of hydrolysis reactor (hydraulic retention time (HRT) 5 d, 35 °C) and methanogenesis reactor (HRT 9 d, 35 °C). The addition of oyster shells led to hydrolysis of 40.33% ± 3.1% of the carbon, whereas alkali reactor hydrolysed almost half (48.68% ± 1.4%). In methanogenesis stage, the highest methane yield under pH adjustment by oyster shells was 580 mL/gVS; 51.05% of the carbon in methanogenesis reactor was converted into methane, generating 1.49–2.00 kWh/kgVS of energy. In comparison, methane yield with NaOH as an alkali was higher (667 mL/gVS), and 59.71% of the carbon was converted into methane, generating 1.97–2.55 kWh/kgVS of energy. To facilitate the digestion of hydrolysate produced using NaOH, we had to remove excess sludge because of sludge accumulation, whereas this was not necessary in oyster-shell treatment. Although NaOH conditioner had higher methane production performance, the oyster-shell conditioner can function as a buffer that regulates itself to keep the pH of the reactor stable with a rapid increase in the hydrogen-ion concentration.

Techno-economic assessment of subcritical water hydrolysis process for sugars production from brewer’s spent grains

Breweries generate a high amount of brewer’s spent grains (BSG), which is a valuable feedstock for industrial applications. In the current study, a techno-economic assessment of the flow-through subcritical water hydrolysis reactor to produce sugars from BSG was performed. Simulations were done for a sequential hydrolysis process in three-extractor vessels of 10 L (pilot-plant) and 500 L (industrial-plant), coupled or not to a separation system. The sugar separation system was composed of a five-zone simulated moving bed (SMB) process. A study on the cost of manufacturing (COM), profitability indicators, and sensitivity analysis was conducted to verify the project feasibility. Moreover, the mass and energy balance of the industrial process was accomplished to evidence the main operational parameters. Simulation results indicated that the scale-up process from pilot to industrial scale reduced the COM by approximately 80 %. In the process coupled with the SMB separation system, arabinose and galactose represented 83.68 % of the costs for sugars separation. Arabinose COM decreased from 64.10 USD kg–1 in pilot-plant to 7.22 USD kg–1 in industrial-plant. The implementation of a separation system recovering six sugars with high added-value can be an advantage in the industrial-plant process when comparing to the process without SMB process, which produces a single hydrolysate fraction with low commercial value. Finally, the integrated subcritical water hydrolysis of BSG coupled with a separation system can be a promising alternative to produce different concentrated sugars in a biorefinery concept.

Process design and exergy cost analysis of a chemical looping ammonia generation system using AlN/Al2O3 as a nitrogen carrier

Chemical looping ammonia generation (CLAG), in which the N2 fixation and hydrolysis reactions occur via the circulation of nitrogen carriers, has the advantages of low-pressure, low energy consumption and high ammonia yield. Therefore, CLAG is considered as a promising alternative to conventional Haber–Bosh technology. In this work, a model for the CLAG system with a capacity of 300,000 t/a is first established. For the simulation, the N2 fixation and hydrolysis reactors are modeled as the kinetics-based mixed flow reactor, and AlN/Al2O3 is used as the nitrogen carrier. The optimal operation conditions of the CLAG system are then determined by sensitivity analyses. The distribution of the exergy loss is gained from exergy analysis. The results showed that the exergy efficiency of the system reached to about 26%. Finally, exergy cost analysis is conducted to evaluate the cost formation of the system. Generally, the unit exergy cost of heat exchangers is larger than those of the other components. The distillation tower in air separation unit, the N2 fixation reactor, and the compressor in compression and purification unit should be primarily considered in system improvement because of the significant effects of their irreversibilities on other components.

Kinetics of hydrolysis of microalgae biomass during hydrothermal pretreatment

Hydrothermal pretreatment is an efficient method for increasing the biogas yield and the amount of energy generated via the anaerobic digestion of microalgae biomass. Few studies have investigated the effects of pretreatment conditions on the rate of the hydrolysis of microalgae biomass into carbohydrates and proteins and the changes in hydrolysis residues, which significantly limit further performance enhancement. In this study, we analyzed the effects of pretreatment conditions on the hydrolysis characteristics and rate of microalgae biomass hydrolysis into carbohydrates and proteins. The results revealed that the yields of soluble carbohydrates and proteins increased with increasing pretreatment temperature and retention time. Conversely, the yields remained unchanged as the mass fraction of microalgae biomass in the microalgae slurry increased from 1% to 10%. The activation energies for the hydrolysis of microalgae biomass into carbohydrates and proteins were 35.07 and 39.66 kJ/mol, respectively. During hydrothermal pretreatment, organic matter within microalgae biomass was converted into relatively small molecules with poor stability, and hydrolysis exposed the major functional groups of microalgae biomass. This study provides guidance for controlling the hydrolysis reaction, designing hydrolysis reactors, and predicting the yields of carbohydrates and proteins.

Assessment of hyper-thermophilic/mesophilic temperature-phased anaerobic co-digestion of crude glycerine and sewage sludge

Temperature-phased anaerobic digestion is considered to be a valuable alternative to achieve new challenges in Wastewater Treatment Plants (WWTP) and biomethane production. This system makes it possible to remove/separate gas toxicants (mainly H2S) in the first phase reactor gas flow (hydrolysis reactor) and improve the profitability of the upgraded biogas flow obtained in the second phase reactor (methanogenic) (i.e. injection into the natural gas grid, vehicle fuel, biogas fuel cell or solid oxide fuel cell quality). The purpose of this study is to investigate the temperature-phased (hyper-thermophilic/mesophilic) anaerobic co-digestion of crude glycerine (CG) and sewage sludge (SS) in semi-continuous reactors. Specifically, to determine the effect of temperature-phased in: i) the quantity and quality of biogas production and ii) the effect on dewatering properties of the digestate obtained in comparison with conventional mesophilic systems. Results show that with a feed composed of 95% SS and 5% CG, the hyper-thermophilic/mesophilic system presents an increase in VSrem (Volatile solids removed) of 5.6% in comparison to the conventional mesophilic system. In reference to biogas quality, the hyper-thermophilic/mesophilic system presents a H2S content decrease of >67% in comparison to the control mesophilic reactor. Moreover, an energy balance shows that the proposed system reaches up to 68% extra heat production in comparison to the conventional mesophilic anaerobic system.

Multi-objective optimization of a 1G-2G biorefinery: A tool towards economic and environmental viability

First-generation sugarcane ethanol production is a well-established technology. However, second-generation ethanol is not yet consolidated in industries. Under these circumstances, this work presents a multi-objective optimization of this process focusing on economic and environmental objectives. The impact of the Brazilian decarbonization program on an integrated biorefinery is analyzed, considering a first-generation ethanol conventional autonomous distillery and a second-generation process with hydrothermal pre-treatment, enzymatic hydrolysis and fermentation of the xylose liquor. The economic metric was the Net Present Value and the environmental assessment was based on the plant inventory considering Global Warming Potential. A multi-objective particle swarm optimization algorithm was used, considering the ratio of bagasse diverted to the second-generation process, enzyme loading and solid fraction in the hydrolysis reactor as optimization variables. The carbon credit price was estimated for each point in the Pareto set in order to make the process economically feasible. As the main conclusions, there is a trade-off between economic and environmental targets, indicating that carbon credits may be essential for second-generation ethanol economic feasibility. The optimized integrated biorefinery is able to increase ethanol production by approximately 24% compared to first-generation biorefineries, but an increase in ethanol production higher than 13% would make the process economically unfeasible, while the decarbonization credits are not being commercialized. A price of $ 15.77 for decarbonization credits would make it possible to produce 20% more ethanol, keeping the integrated biorefinery economically feasible.

Long-term operation of the pilot scale two-stage anaerobic digestion of municipal biowaste in Ho Chi Minh City

A pilot-scale two-stage anaerobic digestion system, which includes a feed tank (0.4 m3), a hydrolysis reactor (1.2 m3) followed by a methane fermenter (4.0 m3) was set up and run at the municipal solid waste landfill located in Ho Chi Minh City (HCMC), Vietnam. The feed that was separated from urban organic solid waste was collected at households and restaurants in District 1, HCMC. This study aimed to investigate the resource recovery performance of the pilot two-stage anaerobic digestion system, in terms of carbon recovery via biogas production and nutrient recovery from digestate. The average organic loading rate (OLR) of the system was step increased from 1.6 kg volatile solids (VS)·m−3·d−1, 2.5 kg VS·m−3·d−1 and 3.8 kg VS·m−3·d−1 during 400 days of operation. During the long-term operation at three OLRs, pH values and alkalinity were stable at both hydrolysis and methanogenesis stages without any addition of alkalinity for the methanogenesis phase. High buildup of propanoic acid and total volatile fatty acid concentrations in the fermenter did not drop pH values and inhibit the methanogenic process at high OLRs (2.5–3.8 kg VS m−3·d−1). The obtained total chemical oxygen demand (tCOD) removal performance was 83–87% at the OLRs ranging from 2.5 kg VS·m−3·d−1 and 3.8 kg VS·m−3·d−1, respectively. The highest biogas yield of 263 ± 64 L·kg−1 tCOD removed obtained at OLR of 2.5 kg VS·m−3·d−1. It is expected that a full scale 2S-AD plant with capacity of 5200 tons day−1 of biowaste collected currently from municipal solid waste in HCMC may create daily electricity of 552 MWh, thermal energy of 630 MWh, and recovery of 16.1 tons of NH4+-N, 11.4 tons of organic-N, and 2.1 tons of TP as both organic liquid and solid fertilizers.