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Four moles of lithium react per mole of iron disulfide. Using molar masses $M_{\mathrm{Li}}=6.94\mathrm{g}\mathrm{mo}{\mathrm{l}}^{-1}$, $M_{\mathrm{Fe}}=55.845\mathrm{g}\mathrm{mo}{\mathrm{l}}^{-1}$ and $M_{\mathrm{S}}=32.06\mathrm{g}\mathrm{mo}{\mathrm{l}}^{-1}$ givesThus the stoichiometric mass ratio is Li:FeS₂ = 1:4.322, or approximately 18.79 wt% lithium and 81.21 wt% iron disulfide within the combined active reactants. This excludes electrolyte, current collectors, casing and any deliberate excess of one reactant. The underlying conversion reaction, rather than the nominal cell voltage, sets that ratio.^[ref]

A charged colloid in a polar electrolyte is surrounded by an electric double layer. For a negatively charged surface, counterions are positive and co-ions negative; their distributions reverse for a positive surface. A compact Stern layer contains specifically adsorbed or closely approaching ions, followed by a diffuse layer where electrostatic attraction competes with thermal motion. Mobile charge integrated over the surroundings balances the particle charge in an overall neutral system.

For a mean-field dilute electrolyte, $n_i(r)=n_{i,\infty }\exp [-z_{i}e\psi (r)/(k_{B}T)]$ with Poisson's equation relates charge density and potential. At weak potential, the diffuse potential outside a sphere decays approximately as $\psi (r)\propto e^{-\kappa (r-a)}/r$. The inverse screening length obeys ${\kappa }^2=e^2{\sum }_i{z}_i^2{n}_{i,\infty }/(ϵk_{B}T)$: added salt shortens the Debye length. The zeta potential is the potential at the hydrodynamic slip plane, not necessarily the surface potential. The simple model neglects ion size, correlations and chemical charge regulation; a polar solvent with almost no dissociated ions need not provide a short screening length.

In generic resistive-pulse sensing, two electrolyte reservoirs are connected through a small aperture. Electrodes apply a bias and a low-noise current amplifier records the pore current. Passage of a weakly charged insulating particle excludes conducting liquid, usually increasing resistance and giving a transient current decrease at fixed voltage. Pulse amplitude, duration and event rate contain size-, transport- and concentration-dependent information, subject to calibration.

Advantages include label-free single-particle counting, electrical readout and small active volume. Limitations include clogging, electrode/pore noise, finite bandwidth, uncertain particle trajectories and surface-conduction effects; a pulse is not intrinsically chemically specific. Strong particle charge or concentration polarization can complicate, or even reverse, the simple blockade signal. The schematic below uses only generic nonbiological particle transport.

charge stabilization of colloids supplies repulsion when like-charged surfaces and their electric double layers approach. steric stabilization uses attached or adsorbed molecular layers whose overlap costs conformational and osmotic free energy. Combining both gives electrosteric stabilization; a solvated coating must remain attached and well solvated. A viscous medium slows encounters but does not by itself create an equilibrium repulsive barrier.

DLVO theory adds screened electrostatic repulsion to Van der Waals force. A representative close-gap form isfor equal spheres of radius $a$, with Hamaker constant $A_H$ and inverse Debye–Hückel screening length $\kappa$. The formula is schematic near molecular contact, where hydration, surface roughness and finite ion size matter. A repulsive barrier many $k_{B}T$ high produces kinetic stability even if the primary attractive minimum is deeper than the dispersed state. Entry into that primary minimum generally gives strongly bound aggregation; a shallow secondary minimum can give reversible flocculation.

Adding electrolyte increases $\kappa$, shortens the repulsion and can remove the barrier, enabling fast diffusion-limited aggregation. The critical coagulation concentration is the approximate salt concentration at which this rapid-coagulation regime begins under specified conditions. It is not a universal property of the salt alone. Test the prediction using time-resolved dynamic light scattering or turbidity at controlled particle concentration, pH and temperature; check that added ions do not specifically adsorb or change the surface chemistry.

An ordinary capacitor stores energy by separating charge across a dielectric: $E=C{V}^2/2$ and $Q=CV$. Electronic charge redistribution is rapid, giving high specific power, but the dielectric breakdown field and modest capacitance limit specific energy. Series resistance limits pulse power and produces heating; a large nominal capacitance does not remove those losses.

A supercapacitor has a much larger interfacial area and nanometre-scale charge separation. An electric double-layer capacitor stores charge without a bulk redox transformation; pseudocapacitance adds sufficiently fast surface or near-surface redox storage. ion motion in pores, electrolyte stability and series resistance constrain its response. Its specific energy usually exceeds an ordinary capacitor's while high specific power and cycling durability remain possible.

An electric battery stores chemical free energy through coupled electrode oxidation-reduction reactions. It can store substantial energy per mass, but charge transfer, ionic transport, diffusion and heat removal constrain rapid discharge. The terminal voltage and accessible capacity depend on discharge rate and state of charge. Accordingly the plotted order follows the storage and transport mechanisms; it is not a claim that every battery has less power than every supercapacitor.

For an ideal dilute electrolyte with molar ionic strength $I=\frac{1}{2}{\sum }_i{c}_i{z}_i^2$, measured in $\mathrm{mol}{\mathrm{L}}^{-1}$, the Debye–Hückel screening length isTaking water's relative permittivity as approximately $78.5$ at $25^{\circ }\mathrm{C}$, $I=0.10\mathrm{M}$ for NaCl. Therefore ${\kappa }^{-1}\simeq 0.96\mathrm{nm}$. This is an exponential screening length, not a hard outer edge of the diffuse layer. The factor of $1000$ converts molarity into $\mathrm{mol}{\mathrm{m}}^{-3}$.

In a galvanic cell, a spontaneous oxidation-reduction reaction supplies electrical work: ${\Delta }_{r}G<0$ for discharge, the anode is negative, and the cathode positive. A discharging electric battery and a hydrogen–oxygen fuel cell are two practical examples. The first stores its reactants internally; the second is supplied continuously with fuel and oxidant.

An electrolytic cell consumes externally supplied electrical work to drive electrode reactions or material transfer under an applied potential. Its anode is positive and cathode negative. water electrolysis for hydrogen production and metal electroplating are two practical examples. oxidation always occurs at the anode and reduction at the cathode in both cell types; the electrode signs change. The electrolyte conducts ions, while electrons flow through the external circuit. A rechargeable battery can operate in either regime depending on whether it is discharging or being charged.

The critical coagulation concentration is the electrolyte concentration at which rapid, approximately diffusion-limited colloidal coagulation begins: the electrostatic barrier has become ineffective and nearly every sufficiently close encounter sticks. It is an operational threshold for the specified colloid and electrolyte, not a universal concentration or a guarantee of a mathematically exact zero barrier in every system.

An alkaline zinc-air battery combines a porous Zn negative electrode, aqueous KOH, an ion-permeable separator and a gas-diffusion positive electrode. At discharge, oxygen is reduced at the air electrode:Zinc oxidation can be written $\mathrm{Zn}+4{\mathrm{OH}}^{-}\to {\mathrm{Zn}(\mathrm{OH})}_4^{2-}+2e^{-}$, followed by ZnO precipitation and hydroxide regeneration. The net reaction is $2\mathrm{Zn}+{\mathrm{O}}_2\to 2\mathrm{ZnO}$.

High energy requires high accessible Zn loading and low inactive mass; high power requires short ion paths, good electronic conduction and a large catalytically active gas/electrolyte/electron interface. A porous hydrophobic gas-diffusion layer admits oxygen while controlling electrolyte flooding and drying. Zn morphology and electrolyte composition must avoid premature passivation, excessive corrosion and hydrogen evolution; atmospheric CO2 can carbonate the alkaline electrolyte. A very high loading can impair transport, so energy and power must be optimized together.

Electrical recharge is possible, but is not guaranteed by a primary Zn-air design. It requires reversible Zn deposition with controlled morphology and an oxygen electrode that can evolve oxygen efficiently without rapid catalyst or support corrosion. Dendrites, shape change, ZnO redistribution, gas evolution and large oxygen-reaction overpotentials limit cycling. Bifunctional oxygen catalysts, or separate oxygen-reduction and oxygen-evolution electrodes, help. Mechanical replacement of spent Zn is a different form of refuelling.^[ref]

A lead-acid battery is suitable. Its positive electrode reduces PbO2 to PbSO4 and its negative electrode oxidizes Pb to PbSO4. The net discharge reaction isUsing the supplied rounded potentials gives $E^{\circ }=1.70-(-0.35)=2.05\mathrm{V}$. The Nernst equation, taking solid and water activities as unity, givesAt $\mathrm{pH}=1$ and $298\mathrm{K}$,Thus $1.93\mathrm{V}$ if sulfate activity is assumed unity. The pH alone does not specify sulfate activity, particularly where bisulfate formation and nonideal concentrated acid matter; without that assumption the numerical voltage is underdetermined.

For recharge, reverse both electrode reactions without irreversible loss of active material. Use porous, electronically connected Pb and PbO2 on acid-compatible conducting grids, with enough pore volume for PbSO4 formation and electrolyte transport. Fine, reversible sulfate deposits are desirable; coarse persistent crystals cause sulfation. The separator must remain acid-resistant, electronically insulating and permeable to electrolyte ions while preventing shorts; selective ion exchange is not intrinsically required. A compatible lead-alloy grid is preferable to assuming any metallic substrate survives the positive electrode's oxidizing acidic environment. Control current and charging voltage to limit hydrogen evolution, oxygen evolution, water loss, corrosion, heating and active-material shedding. Nickel hydroxide-based alkaline electrodes are poor choices in this acidic electrolyte because their phase stability and reaction conditions differ from those of their tabulated alkaline half-reactions.

Two electrons are transferred per formula unit of Li2O2. Its theoretical specific capacity isAt $3\mathrm{V}$, the corresponding theoretical specific energy is $3q=3.50\mathrm{Wh}{\mathrm{g}}^{-1}$, or $3500\mathrm{Wh}\mathrm{k}{\mathrm{g}}^{-1}$. The mass basis is Li2O2, equivalently the combined stoichiometric masses of consumed Li and O2; a value normalized to Li metal alone would be different.

A real lithium-air battery also includes electrolyte, porous positive-electrode support, separator, current collectors, excess reactants, packaging and possibly oxygen treatment. Insulating Li2O2 can block pores and electron transport, limiting utilization; polarization, electrolyte decomposition, moisture/CO2 contamination and parasitic reactions lower useful voltage and reversible capacity. A lithium-ion battery instead shuttles Li ions between pre-existing host electrodes, generally in a closed cell without consuming atmospheric oxygen; the oxygen/peroxide reaction and its mass/transport requirements make the Li-air mechanism distinct.

Use a lithium-metal negative electrode and a carbon-monofluoride composite positive electrode, separated by a porous, electrically insulating battery separator wetted by a lithium-salt electrolyte in a suitable nonaqueous solvent. Conducting carbon and a binder provide electronic contact through the fluorinated-carbon electrode to its electric current collector; the lithium electrode has its own electric current collector. A sealed stacked or wound assembly supplies useful area and contains the electrolyte.

During discharge lithium is the anode and the carbon-monofluoride composite is the cathode. lithium ions move through the electrolyte while electrons flow through the external load. The battery separator prevents electronic shorting while permitting ionic transport. An aqueous electrolyte is unsuitable because metallic lithium reacts with water. The requested very long operating time requires enough active material and low self-discharge, not merely a high nominal voltage.

The reaction consumes one mole of CF for each mole of electrons. Using $M_{\mathrm{CF}}=12.01+19.00=31.01\mathrm{g}\mathrm{mo}{\mathrm{l}}^{-1}$,This is active CF alone for the same single-cell-equivalent assumption, not the full positive-electrode or pack mass. Conductive additive, binder, electrolyte, battery separator, collectors and casing add mass, and incomplete utilization increases the required CF.

This is a primary cell and should not be treated as rechargeable. Discharge converts the fluorinated-carbon electrode into carbon and lithium fluoride. It does not simply insert lithium into a host that can be reversibly deintercalated. Reversing electric current does not cleanly reconstruct the original distributed C–F bonding and electrode microstructure.

Insulating LiF, loss of the original reaction interfaces and unwanted electrolyte reactions obstruct reversibility. Replating lithium can also produce an irregular metallic deposit and internal shorting. A thermodynamically possible formal reverse reaction is therefore not evidence of a practical rechargeable cell.

Increase the electrochemically accessible area and reduce transport resistance rather than merely forcing more electric current through the same thick electrode. A thinner, porous composite distributed over a larger area, a conductive-carbon network, good electrolyte wetting and short ionic paths reduce local current density and electric polarization. Adequate battery separator conductivity and low-resistance collectors also help. Parallel cells can distribute total electric current while retaining the total active-material inventory.

The objective is to preserve usable capacity at a higher rate by avoiding premature voltage cutoff and inaccessible active material. It does not create more charge: a fixed inventory with $175.2\mathrm{Ah}$ delivers a greater electric current for a proportionally shorter time. Maintaining the original two-year duration at greater electric current requires proportionally more capacity.

Clean and degrease the nickel surface, remove its inhibiting oxide by an appropriate brief surface treatment, rinse, and immerse it in an aqueous bath containing reducible gold(III) species. Control concentration, temperature and immersion time, then rinse after the desired deposition. A solution of a gold complex is practical, but its actual reduction potential must be evaluated for that complex and bath: it need not equal the supplied free-ion standard potential.

At anodic sites nickel dissolves as $\mathrm{N}{\mathrm{i}}^{2+}$, releasing electrons into the conducting substrate. Those electrons reduce gold ions at cathodic sites, nucleating and growing metallic gold. The nickel itself is the reducing agent, so no external electrical supply or separate reducing reagent is required. The coupled electron balance is three nickel atoms dissolved for two gold atoms deposited for the stated oxidation states.

The process can slow or stop when a sufficiently continuous gold coating prevents the electrolyte from reaching nickel. This is not an absolute thickness rule: pores, cracks or exposed edges preserve nickel dissolution and allow continued deposition, sometimes with undercutting. nickel passivation, depletion of gold ions near the surface, diffusion through a porous layer, bath speciation and competing reactions also affect the rate. Dense gold coverage and porous gold coverage therefore have very different limiting behavior.

Flocculation indicates that the attraction/kinetic balance has changed: electrolyte may screen a double-layer barrier; pH may reduce surface charge; multivalent ions can promote aggregation; added polymer can bridge particles or cause depletion force; poor solvent conditions can collapse stabilizing layers. Rapid evaporation concentrates both particles and salts and can force contacts faster than they anneal. Aggregates then sediment much faster because their effective buoyant size has grown.

Check ionic strength, pH, surface charge and the particle size distribution before and during assembly. Dialyse or reduce salt where appropriate, restore surface charge, add a nonbridging steric stabilization with a compatible solvent, and slow the concentration step. Compare untreated and deliberately salt-screened controls. Restoring repulsion after irreversible aggregation may not redisperse the particles, so prevention is preferable to assuming all settled material can be recovered.

A conventional capacitor stores separated electronic charge across a dielectric, with capacitance set approximately by $C=\epsilon A/d$. An electric double-layer capacitor stores charge at the interface between a porous electronic conductor and an ionic electrolyte. Electrolyte counterions screen charge on the electrode over a very small interfacial separation, and a porous electrode provides a large accessible area. The separator prevents an electronic short while permitting ionic transport; the two electrode interfaces form series capacitances.

Pseudocapacitance is charge storage by fast, reversible Faradaic processes that give a capacitor-like relation between stored charge and potential over a useful range. Examples include surface redox and suitably rapid insertion processes. It is distinct from purely electrostatic double-layer charging. Merely observing a redox peak does not establish pseudocapacitive behaviour: a slow two-phase battery reaction can remain battery-like even when its electrode is nanostructured.

For an ideally dissociated electrolyte, the Debye–Hückel screening length isHere $n_i$ is ionic number density, $z_i$ the charge in units of the elementary charge, and $c_i$ is molar concentration. Conversion between $I$ and number density cancels in a ratio. At fixed relative permittivity, ${\lambda }_D\propto \sqrt{T/I}$.

In $0.01\mathrm{M}$ sodium chloride, $c_{\mathrm{N}{\mathrm{a}}^{+}}=c_{\mathrm{C}{\mathrm{l}}^{-}}=0.01\mathrm{M}$, giving $I_1=0.01\mathrm{M}$. Complete dissociation of $0.1\mathrm{M}$ aluminium chloride gives $c_{\mathrm{A}{\mathrm{l}}^{3+}}=0.1\mathrm{M}$ and $c_{\mathrm{C}{\mathrm{l}}^{-}}=0.3\mathrm{M}$, soThe factor is sixty, not ten: the squared charge and the three counterions per formula unit both matter. Using the given $5\mathrm{nm}$ reference length directly, and $T_1\simeq 298\mathrm{K}$, $T_2=323\mathrm{K}$,The modest temperature increase raises the screening length by only about $4\%$ at fixed concentration; the large increase in ionic strength shortens it by almost an order of magnitude overall.

Under charge stabilization of colloids, the electrostatic double-layer repulsion now has a much shorter range. Attractive Van der Waals forces can then dominate at closer separations, reducing the barrier to particle aggregation in DLVO theory. Thus an electrostatically stabilized colloid is likely to be destabilized, with aggregation more likely than in the original dispersion.

This is a conditional physical prediction, not a proof of instability from a length alone. No particle radius, surface potential, attractive interaction strength or steric coating is specified. Steric stabilization could preserve stability, and trivalent-ion adsorption can alter the surface charge. Moreover, ideal screening theory is only an estimate at $I\simeq 0.6\mathrm{M}$, where ion association, hydrolysis and activities can matter. The numerical result uses the supplied reference length and the stipulated unchanged permittivity, rather than replacing either with an unprovided calibration.

A salt bridge is an ionic connection between electrolyte compartments that limits bulk mixing while permitting electric charge transport. Its mobile ions compensate changes caused by the electrode half-reactions, keeping the bulk chemical solutions approximately electrically neutral during sustained electric current. It does not conduct electrons like the external wire, and its ions need not be consumed at either electrode. The ionic return path and compensating ion flows are explained in Purdue University, Electrochemical Reactions: salt bridge and charge balance.

In a discharging Daniell cell, anions moving toward the anode compartment and cations moving toward the cathode compartment both contribute to the internal conventional current from anode toward cathode. This charge-balance role is compatible with a negative anode: terminal signs do not imply that the whole anode chemical solution is negatively charged. The simple compensating-inventory example in Daniell cell does not fix all individual ion fluxes; diffusion and the cell's other mobile ions can contribute. A real bridge also introduces electrical resistance and may introduce a junction electric potential difference, so its presence does not guarantee an exact thermodynamic cell reading. See IUPAC Gold Book: salt bridge and liquid-junction potential.