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Processes 2018, 6, 59 4 of 14 where Q∞ is the adsorption capacity at the final time(mg·L−1); De is the diffusion coefficient (cm2·s−1); and r is the particle size of the adsorbent (cm). The pseudo-first-order kinetic model (Equation (3)) and the pseudo-second-order kinetic model (Equation (4)) were used to simulate the saturated adsorption curve, aimed to confirm the kinetic constant of the adsorption process. K1 lg(Qe−Qt)=lgQe− 2.303 ×t (3) t = 1 × 1 + 1 ×t (4) Qt K2 Q2e Qe where Qe is the adsorption capacity when it reaches the adsorption equilibrium (mg·L−1); Qt is the adsorption capacity calculated with Equation (1); K1 is the adsorption rate constant of the pseudo-first-order kinetic model; and K2 is the adsorption rate constant of pseudo-second-order kinetic model. 2.3.3. Adsorption Isotherm Test The lithium ion adsorption behavior test was measured on HMO (0.04, 0.075, 0.11, 0.15 and 0.19 g) in 500 mL initial concentrations (10, 20, 30, 40 and 50 mg·L−1 LiCl·H2O solution) were added to five flasks respectively, (Ph = 10, adjusted by a buffer solution composed of 0.1 mol·L−1 NH4Cl and 0.1 mol·L−1 NH4OH). The flasks were shaken on a shaker at 200 rpm at 18 ◦C for 12 h. The adsorption isotherm curve is fitted according to the following isotherm models: Langmuir isotherm model: Qe1 = Qm ×KL ×Ce (5) 1+KL ×Ce Freundlich isotherm model: where Qm is the theoretically calculated maximum adsorption capacity; KL is the Langmuir constant; KF is the Freundlish constant; and n is an empirical constant. 2.4. Selective Adsorption Behavior The selectivity of lithium ions compared with other coexisting ions in brine was adjusted pH value to 10 by 0.1 mol·L−1 NH4OH, carried out by stirring (200 rpm) 0.1 g ion sieve in 20 mL saline brine at 20 ◦C for 72 h. The adsorption capacity of metal ion at equilibrium (Qe), distribution coefficient (K ), separation factor (αLi ) and concentration factor (C ) are calculated according to the d Me F αLi = K Me Kd = C0,Me − Ce,Me × V/(Ce,Me × W) (7) /K (Me = K+, Ca2+, Na+, Mg2+, Li+) (8) d,Me Q =K×C1/n (6) e2 F e following equations: where C0, Me is the initial concentrate of ions in brine (mg·L−1); Ce, Me is the final concentrate of ions in brine after adsorption (mg·L−1); V is the volume of solution (L); W is the weight of the HMO ion sieve (g); Qe, Me is the saturated adsorption capacity of ions in brine (mg·g−1). 2.5. Desorption Behavior LMO was renamed LMO-1 after the Li+ adsorption of the HMO. The curve of the Li+ extraction and manganese dissolution was carried out by stirring (200 rpm) 0.1 g LMO-1 in 500 mL hydrochloric d,Li CF = Qe,Me/C0,Me (Me = K+, Ca2+, Na+, Mg2+, Li+) (9)PDF Image | Sieves for Highly Selective Li Adsorption
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ORC Waste Heat Turbine and ORC System Build Plans: All turbine plans are $10,000 each. This allows you to build a system and then consider licensing for production after you have completed and tested a unit.Redox Flow Battery Technology: With the advent of the new USA tax credits for producing and selling batteries ($35/kW) we are focussing on a simple flow battery using shipping containers as the modular electrolyte storage units with tax credits up to $140,000 per system. Our main focus is on the salt battery. This battery can be used for both thermal and electrical storage applications. We call it the Cogeneration Battery or Cogen Battery. One project is converting salt (brine) based water conditioners to simultaneously produce power. In addition, there are many opportunities to extract Lithium from brine (salt lakes, groundwater, and producer water).Salt water or brine are huge sources for lithium. Most of the worlds lithium is acquired from a brine source. It's even in seawater in a low concentration. Brine is also a byproduct of huge powerplants, which can now use that as an electrolyte and a huge flow battery (which allows storage at the source).We welcome any business and equipment inquiries, as well as licensing our turbines for manufacturing.CONTACT TEL: 608-238-6001 Email: greg@infinityturbine.com (Standard Web Page)