Patent Application
20230352656
This invention relates in general to electroactive materials that are suitable for use in electrodes for rechargeable metal-ion batteries, and more specifically to particulate materials having high electrochemical capacities that are suitable for use as anode active materials in rechargeable metal-ion batteries.
Rechargeable metal-ion batteries are widely used in portable electronic devices such as mobile telephones and laptops and are finding increasing application in electric or hybrid vehicles. Rechargeable metal-ion batteries generally comprise an anode in the form of a metal current collector provided with a layer of an electroactive material, defined herein as a material which is capable of inserting and releasing metal ions during the charging and discharging of a battery. The terms “cathode” and “anode” are used herein in the sense that the battery is placed across a load, such that the anode is the negative electrode. When a metal-ion battery is charged, metal ions are transported from the metal-ion-containing cathode layer via the electrolyte to the anode and are inserted into the anode material. The term “battery” is used herein to refer both to a device containing a single anode and a single cathode and to devices containing a plurality of anodes and/or a plurality of cathodes.
There is interest in improving the gravimetric and/or volumetric capacities of rechargeable metal-ion batteries. To date, commercial lithium-ion batteries have largely been limited to the use of graphite as an anode active material. When a graphite anode is charged, lithium intercalates between the graphite layers to form a material with the empirical formula LixC6 (wherein x is greater than 0 and less than or equal to 1). Consequently, graphite has a maximum theoretical capacity of 372 mAh/g in a lithium-ion battery, with a practical capacity that is somewhat lower (ca. 340 to 360 mAh/g). Other materials, such as silicon, tin and germanium, are capable of intercalating lithium with a significantly higher capacity than graphite but have yet to find widespread commercial use due to difficulties in maintaining sufficient capacity over numerous charge/discharge cycles.
Silicon in particular has been identified as a promising alternative to graphite for the manufacture of rechargeable metal-ion batteries having high gravimetric and volumetric capacities because of its very high capacity for lithium (see, for example, Insertion Electrode Materials for Rechargeable Lithium Batteries, Winter, M. et al. in Adv. Mater. 1998, 10, No. 10). At room temperature, silicon has a theoretical maximum specific capacity in a lithium-ion battery of about 3,600 mAh/g (based on Li15Si4). However, the intercalation of lithium into bulk silicon leads to a large increase in the volume of the silicon material of up to 400% of its original volume when silicon is lithiated to its maximum capacity. Repeated charge-discharge cycles cause significant mechanical stress in the silicon material, resulting in fracturing and delamination of the silicon anode material. Volume contraction of silicon particles upon delithiation can result in a loss of electrical contact between the anode material and the current collector. A further difficulty is that the solid electrolyte interphase (SEI) layer that forms on the silicon surface does not have sufficient mechanical tolerance to accommodate the expansion and contraction of the silicon. As a result, newly exposed silicon surfaces lead to further electrolyte decomposition and increased thickness of the SEI layer and irreversible consumption of lithium. These failure mechanisms collectively result in an unacceptable loss of electrochemical capacity over successive charging and discharging cycles.
A number of approaches have been proposed to overcome the problems associated with the volume change observed when charging silicon-containing anodes. It has been reported that fine silicon structures below around 150 nm in cross-section, such as silicon films and silicon nanoparticles are more tolerant of volume changes on charging and discharging when compared to silicon particles in the micron size range. However, neither of these is suitable for commercial scale applications in their unmodified form; nanoscale particles are difficult to prepare and handle and silicon films do not provide sufficient bulk capacity.
WO 2007/083155 discloses that improved capacity retention may be obtained with silicon particles having high aspect ratio, i.e. the ratio of the largest dimension to the smallest dimension of the particle. The small cross-section of such particles reduces the structural stress on the material due to volumetric changes on charging and discharging. However, such particles may be difficult and costly to manufacture and can be fragile. In addition, high surface area may result in excessive SEI formation, resulting in excessive loss of capacity on the first charge-discharge cycle.
It is also known in general terms that electroactive materials such as silicon may be deposited within the pores of a porous carrier material, such as an activated carbon material. These composite materials provide some of the beneficial charge-discharge properties of nanoscale silicon particles while avoiding the handling difficulties of nanoparticles. Guo et al. (Journal of Materials Chemistry A, 2013, pp.14075-14079) discloses a silicon-carbon composite material in which a porous carbon substrate provides an electrically conductive framework with silicon nanoparticles deposited within the pore structure of the substrate with uniform distribution. It is shown that the composite material has improved capacity retention over multiple charging cycles, however the initial capacity of the composite material in mAh/g is significantly lower than for silicon nanoparticles.
JP 2003100284 discloses an active material comprising a carbon-based scaffold with small pores branching off from a few larger pores. An electroactive material (e.g. silicon) is indiscriminately located on the walls of both large and small pores and on the external surface of the carbon-based scaffold.
Silicon sub-oxide materials (e.g. SiOx, wherein 0<x<2) have been used in “hybrid” electrodes which comprise predominantly graphite as the active materials. However, due to expansion of the SiOx on lithiation and a relatively high irreversible lithium loss during the first charge cycle, the maximum loading of SiOx is typically around 10 wt% of the total electroactive materials in the electrode. There is therefore a need for high capacity electrode materials that have comparable lithiation capacity to silicon oxides but reduced expansion and reduced capacity loss during the first charge cycle.
The desirable expansion properties of electrode materials must be obtained alongside other important properties. In particular, a commercially viable alternative electrode material needs to provide the benefit of high lithiation capacity alongside with high capacity retention over large numbers of charge-discharge cycles. In addition, it is important that any new electroactive material should be readily substitutable for known materials in conventional electrode fabrication processes. These processes typically rely on calendering of electrode materials onto current collectors in order to densify the electrode layers and to improve space utilisation within a battery design. Porous materials are vulnerable to fracturing during electrode fabrication, resulting in impaired electrochemical performance. It is therefore a particular requirement that new electrochemical materials should have sufficient structural strength alongside increased electrochemical storage capacity and reversible capacity retention.
The present inventors have previously reported the development of a class of electroactive materials having a composite structure in which nanoscale electroactive materials, such as silicon, are deposited into the pore network of a highly porous conductive particulate material, e.g. a porous carbon material.
For example, WO 2020/095067 and WO2020/128495 report that the improved electrochemical performance of these materials can be attributed to the way in which the electroactive materials are located in the porous material in the form of small domains with dimensions of the order of a few nanometres or less. These fine electroactive structures are thought to have a lower resistance to elastic deformation and higher fracture resistance than larger electroactive structures, and are therefore able to lithiate and delithiate without excessive structural stress. As a result, the electroactive materials exhibit good reversible capacity retention over multiple charge-discharge cycles. Secondly, by controlling the loading of silicon within the porous carbon framework such that only part of the pore volume is occupied by silicon in the uncharged state, the unoccupied pore volume of the porous carbon framework is able to accommodate a substantial amount of silicon expansion internally. Furthermore, by locating nanoscale silicon domains within small mesopores and/or micropores as described above, only a small area of silicon surface is accessible to electrolyte and so SEI formation is limited. Additional exposure of silicon in subsequent charge-discharge cycles is substantially prevented such that SEI formation is not a significant failure mechanism leading to capacity loss. This stands in clear contrast to the excessive SEI formation that characterizes the material disclosed by Guo, for example (see above).
It has now been determined that improved electrochemical performance of composite materials comprising silicon and porous carbon can be obtained when the porous carbon material is an activated carbon material derived from certain plant sources. Specifically, it has been identified that improved electrochemical performance can be obtained when the porous carbon material is an activated carbon material formed by the pyrolysis of plant sources containing a high content of lignin. It has further been identified that the performance of these composite materials depends on the way in which the porous carbon material has been activated, with steam or CO2 activation providing a further benefit.
In a first aspect, the invention provides a particulate material comprising a plurality of composite particles, wherein the composite particles comprise:
The invention therefore relates in general terms to a particulate material in which silicon partially occupies the pore volume of a highly porous carbon framework. As used herein, the term “nanoscale silicon domain” refers to a nanoscale body of elemental silicon having maximum dimensions that are determined by the location of the silicon within the micropores and/or mesopores of the porous carbon framework.
The porous carbon framework used according to the invention is a form of activated carbon. The term “activated carbon” as used herein refers to a carbonaceous material that has been physically or chemically processed to increase its porosity and surface area. Chemical activation or physical activation (i.e. high temperature steam or CO2) mechanisms are among common methods used in the production of activated carbons.
The invention is based on the discovery that activated carbon that is produced by the pyrolysis and physical activation (steam or CO2) of a plant source comprising at least 25 wt% lignin (dry weight basis) provides superior electrochemical performance when compared to porous carbon materials derived either from other plant sources, or from non-plant sources (e.g. pyrolysis of polymeric or resinous materials) and/or where chemical (i.e. non-steam or CO2) methods of activation are used to prepare the porous carbon material.
Previous work in this area has focused primarily on the pore volume and pore size distribution of the porous carbon framework as important factors in determining the electrochemical performance of similar materials. For example, it is known in general terms that electroactive materials such as silicon may be deposited within the pores of a porous carbon framework by chemical vapour infiltration (CVI) and that a wide variety of composite particle structures may be obtained through variations in the pore volume and pore size distribution of the porous carbon framework. However, there are other properties of porous carbon materials that can have a significant impact on the form and structure of the nanoscale silicon domains. These include factors such as the shape of the pores and the tortuosity and constrictivity of the pore structures, i.e. features of the pore structure that characterize the ways in which the pore volume is interconnected. It has been found that in porous carbon materials derived from the pyrolysis of plant sources having a high lignin content, these additional features of the pore structure are optimized for the formation of composite particles having a high gravimetric and volumetric capacity as well as high capacity retention over multiple charge-discharge cycles.
Without being bound by theory, it is believed that the pyrolysis of plant sources having a high content of lignin results in a carbonized material having a closer spacing between graphitic platelets than is obtained from other carbon-containing precursor materials (e.g. plant or polymer-based materials). This results in the formation of a high proportion of micropores in the pyrolyzed material. Furthermore, it is thought that the network structure of the pores has a higher degree of tortuosity and constrictivity due to the higher density of lignin in the plant precursor. Physical activation (using steam or CO2) of the pyrolyzed material will then increase the pore volume by removing nano-scale regions of carbon in the pore walls. This enables a moderate level of micro-pore sized spaces to be maintained, accessible by connecting channels whilst attaining a higher overall pore volume.
It is further understood that the combination of a higher density of lignin in the plant precursor and steam or CO2 activation provides a relatively high proportion of “ink-bottle shaped” pores, or more generally, a proportion of (sub-10 nm) mesopore spaces that are only accessible through a narrow opening(s) with a width smaller than that of the mesopore. Ink-bottle shaped pores are where a larger dimensioned pore space is accessible only by an opening that is much smaller. Pore structures such as this are believed to promote the formation of partially filled pore spaces (e.g. the pore walls have a deposited Si coating less than 2 nm depth) followed by blocking (capping) of the opening that prevents the pore space being fully filled with silicon.
In chemical activation methods the plant source materials are impregnated with a chemical activation agent (such as KOH, H3PO4, ZnCl2 etc.). The plant source is typically impregnated prior to pyrolysis and the pyrolysis step takes place simultaneously with the activation, though the plant source may be carbonized prior to chemical impregnation. If the porous carbon is instead formed using chemical activation processes, then, instead of pores being created by removal of carbon, the activation mechanism works by expanding existing pores or pushing apart graphene sheets (exfoliation) which is not conducive to maintaining a high proportion of micro-pore spaces accessible via narrow channels/openings. This is thought to account for the relatively poorer electrochemical performance of composite materials prepared from chemically activated porous carbon materials.
The porous carbon framework therefore comprises a three-dimensionally interconnected open pore network comprising a combination of micropores and/or mesopores and optionally a minor volume of macropores. In accordance with IUPAC terminology, the term “micropore” is used herein to refer to pores of less than 2 nm in diameter, the term “mesopore” is used herein to refer to pores of 2-50 nm in diameter, and the term “macropore” is used to refer to pores of greater than 50 nm diameter.
References herein to the volume of micropores, mesopores and/or macropores in the porous carbon framework, and any references to the distribution of pore volume within the porous carbon framework, refer to the internal pore volume of the porous carbon framework taken in isolation (i.e. in the absence of any silicon or other materials occupying some or all of the pore volume).
The porous carbon framework is preferably derived from a plant source comprising at least 28 wt% lignin, or at least 30 wt% lignin, or at least 35 wt% lignin on a dry weight basis. The higher content of lignin is believed to increase the tortuosity and constrictivity of the pore volume and the proportion of “ink-bottle shaped” pores, as described above.
The plant source is preferably a lignocellulosic material, i.e. a material that comprises both cellulose and/or hemicellulose. Preferably the plant source comprises at least 40 wt%, or at least 45 wt%, or at least 50 wt%, or at least 55 wt%, or at least 60 wt%, or at least 65 wt%, or at least 70 wt% cellulose and/or hemicellulose on a dry weight basis.
More preferably, the plant source is a lignocellulosic material comprising at least 25 wt% lignin and at least 40 wt% cellulose and/or hemicellulose, or at least 25 wt% lignin and at least 45 wt% cellulose and/or hemicellulose, or at least 25 wt% lignin and at least 50 wt% cellulose and/or hemicellulose, or at least 25 wt% lignin and at least 55 wt% cellulose and/or hemicellulose, or at least 25 wt% lignin and at least 60 wt% cellulose and/or hemicellulose, or at least 30 wt% lignin and at least 50 wt% cellulose and/or hemicellulose, or at least 30 wt% lignin and at least 55 wt% cellulose and/or hemicellulose, or at least 30 wt% lignin and at least 60 wt% cellulose and/or hemicellulose.
A variety of different plant-based materials may be used to prepare the porous carbon framework. Examples of plant sources that may be used include the husks and shells of seeds, nuts and fruits (also including drupes, kernels and pits). Examples of these plant sources include the shells and husks of coconuts (including coir), groundnuts, walnuts, apricots, almonds, palm seeds, peaches, olives and hazelnuts. Other plant sources with high lignin content include bamboos and tree barks (e.g. the bark of softwood trees including pine, spruce, larch and poplar, and hardwood trees including oak). A preferred plant source is coconut shells.
The plant source preferably has an elemental composition including at least 40 wt% carbon, at least 3 wt% hydrogen and at least 30 wt% oxygen. Trace amounts of nitrogen, sulphur and chlorine may also be present. More preferably, the plant source has an elemental composition including around 50 wt% carbon, 5 wt% hydrogen and 40 wt% oxygen with lesser amounts of nitrogen, sulphur and chlorine being present.
The porous carbon framework is obtained from the plant source in a process comprising two steps. Firstly, the carbonaceous plant material is pyrolyzed by heating the plant material in an inert atmosphere. Pyrolysis is usually carried out at a temperature of about 400 to 900° C., or about 500 to 700° C., or about 550 to 700° C. so that dehydration and devolatilization of the carbon occur. Preferably, the temperature does not exceed about 700° C. Optionally, the carbonaceous material is pre-treated to remove impurities prior to heating. Optionally, the carbonaceous material is purified and/or washed and dried prior to heating. Optionally, the carbonaceous material is sieved and crushed or milled to obtain uniform sized particles prior to heating. Optionally the carbonaceous material is pelletized before heating.
Secondly, the pyrolyzed material is activated by heating with in a flow of steam or CO2 at a temperature between 600° C. and 1200° C. This allows a chemical reaction between the carbon and steam or CO2 to take place at the internal surface of the carbon, removing carbon from the pore walls and thereby increasing the pore volume. The steam or CO2 activation process allows the pore size to be readily altered producing activated carbons with the desired porosity. Preferably, the pyrolyzed material is activated with steam.
The steam or CO2 activation may suitably be performed in a rotary furnace, a fixed bed reactor or a fluidized bed reactor. Optionally, additional washing, cleaning or purifying steps may be performed after the activation. Optionally the pyrolyzation and activation steps may be combined into a continuous process. Optionally, the activated material is comminuted (e.g. milled) and/or sieved after the activation step to obtain particles of the desired size.
The burn-off of the pyrolyzed material during activation is preferably at least 30%, or at least 40%. The burn-off is preferably no more than 80%, or no more than 75%, or no more than 70%. The burn-off is the mass fraction of the pyrolyzed material that is removed during the physical activation step, as a percentage of the material mass before physical activation is commenced.
Preferably the D50 particle diameter of the porous carbon framework is no more than 30 µm. Optionally the D50 particle diameter may be no more than 25 µm, or no more than 20 µm, or no more than 18 µm, or no more than 16 µm, or no more than 14 µm, or no more than 12 µm, or no more than 10 µm, or no more than 8 µm. Optionally, the D50 particle diameter may be at least 0.5 µm, or at least 1 µm, or at least 1.5 µm, or at least 2 µm.
For instance, the porous carbon framework particles may have a D50 particle diameter in the range from 0.5 to 30 µm, or from 0.5 to 25 µm, or from 1 to 20 µm, or from 1 to 15 µm, or from 1 to 12 µm, or from 1 to 10 µm, or from 1 to 8 µm.
The D10 particle diameter of the porous carbon framework particles is preferably at least 0.1 µm, or at least 0.3 µm, or at least 0.5 µm. The D90 particle diameter of the porous carbon framework particles is preferably no more than 50 µm, or no more than 40 µm, or no more than 30 µm, or no more than 25 µm, or no more than 20 µm, or no more than 15 µm.
The porous carbon framework particles preferably have a narrow size distribution span. For instance, the particle size distribution span (defined as (D90-D10)/D50) is preferably 5 or less, more preferably 4 or less, more preferably 3 or less, more preferably 2 or less, and most preferably 1.5 or less. Preferably, the particle size distribution of the porous carbon framework particles has a positive skew.
By forming the porous carbon framework particles with size distributions as set out herein, it is believed that the presence of large micron-sized pore voids/channels and a large proportion of macro-sized pores that remain after activation from the original cell structures of the plant source material are removed, prior to the chemical infiltration of silicon into the carbon framework. A narrow size distribution span with positive skew and average sphericity above 0.50 will also promote uniform deposition of silicon throughout the full particle size range in the CVI reactor.
The term “particle diameter” as used herein refers to the equivalent spherical diameter (esd), i.e. the diameter of a sphere having the same volume as a given particle, wherein the particle volume is understood to include the volume of any intra-particle pores. The terms “D50” and “D50 particle diameter” as used herein refer to the volume-based median particle diameter, i.e. the diameter below which 50% by volume of the particle population is found. The terms “D10” and “D10 particle diameter” as used herein refer to the 10th percentile volume-based median particle diameter, i.e. the diameter below which 10% by volume of the particle population is found. The terms “D90” and “D90 particle diameter” as used herein refer to the 90th percentile volume-based median particle diameter, i.e. the diameter below which 90% by volume of the particle population is found.
Particle diameters and particle size distributions can be determined by routine laser diffraction techniques in accordance with ISO 13320:2009. Unless stated otherwise, particle size distribution measurements as specified or reported herein are as measured by the conventional Malvern Mastersizer™ 3000 particle size analyzer from Malvern Instruments. The Malvern Mastersizer™ 3000 particle size analyzer operates by projecting a helium-neon gas laser beam through a transparent cell containing the particles of interest suspended in an aqueous solution. Light rays that strike the particles are scattered through angles which are inversely proportional to the particle size and a photodetector array measures the intensity of light at several predetermined angles and the measured intensities at different angles are processed by a computer using standard theoretical principles to determine the particle size distribution. Laser diffraction values as reported herein are obtained using a wet dispersion of the particles in 2-propanol with a 5 vol% addition of the surfactant SPAN™-40 (sorbitan monopalmitate). The particle refractive index is taken to be 2.68 for porous carbon framework particles and 3.50 for composite particles and the dispersant index is taken to be 1.378. Particle size distributions are calculated using the Mie scattering model.
The porous carbon framework particles may have an average sphericity (as defined herein) of more than 0.2, or more than 0.3. Preferably they have an average sphericity of at least 0.4, or at least 0.5, or at least 0.55, or at least 0.65, or at least 0.7.
It is possible to obtain highly accurate two-dimensional projections of micron scale particles by scanning electron microscopy (SEM) or by dynamic image analysis, in which a digital camera is used to record the shadow projected by a particle. The term “sphericity” as used herein shall be understood as the ratio of the area of the particle projection (obtained from such imaging techniques) to the area of a circle, wherein the particle projection and circle have identical circumference. Thus, for an individual particle, the sphericity S may be defined as:
wherein Am is the measured area of the particle projection and Cm is the measured circumference of the particle projection. The average sphericity Sav of a population of particles as used herein is defined as:
wherein n represents the number of particles in the population. The average sphericity for a population of particles is preferably calculated from the two-dimensional projections of at least 50 particles.
The porous carbon framework preferably has an elemental composition including at least 90 wt% carbon, preferably at least 95 wt% carbon, more preferably at least 97 wt% carbon, or at least 98 wt% carbon (measured using Infrared absorption analysis of combustion products). The porous carbon framework may optionally comprise minor amounts of other elements, such as oxygen, nitrogen, sulphur and hydrogen. The elemental composition of the porous carbon framework may be determined by conventional elemental analysis techniques as described herein, performed in the absence of silicon. Carbon, hydrogen and nitrogen content are measured according to ISO 29541. Preferably the porous carbon framework comprises no more than 7 wt% oxygen, more preferably no more than 6 wt%, or no more than 5 wt%, or no more than 3 wt% oxygen. Preferably, the carbon framework comprises less than 0.1 wt% iron, more preferably less than 0.05 wt% iron.
The porous carbon framework preferably has an ash content that is no more than 10 wt%, more preferably no more than 5 wt%, or no more than 3 wt%, or no more than 1.5 wt%, or no more than 1 wt%, or no more than 0.5 wt%. The ash content is the mass of the residue left after full combustion of the porous carbon framework as a percentage of the initial mass, calculated according to ISO 1171.
A porous carbon framework containing high levels of oxygen or other contaminants is believed to lead to reduce performance of the composite product due to interactions with other elements during manufacture of the silicon-carbon composite particles and/or their use in a cell electrode. The ash content provides a measure of the amount of mineral oxides such as silica and alumina remaining after combustion of the carbon.
The total volume of micropores and mesopores (i.e. the total pore volume of pores having a diameter in the range of 0 to 50 nm) is referred to herein as P1 cm3/g, wherein P1 represents a dimensionless number having a value of from 0.5 to 1.5. For the avoidance of doubt, references herein to the pore volume of the porous carbon framework relate (in the absence of any indication to the contrary) to the pore volume of the porous carbon framework in isolation, i.e. as measured in the absence of any electroactive material (or any other material) occupying the pores of the porous carbon framework.
The value of P1 is preferably at least 0.55, or at least 0.6, or at least 0.65, or at least 0.7, or at least 0.75. A higher porosity framework is advantageous since it allows a larger amount of silicon to be accommodated within the pore structure without compromising the resistance of the porous carbon framework to fracturing under compressive stress during electrode manufacture or expansion stress due to lithiation of the silicon. If P1 is too high, however, then it is not possible to achieve the elevated levels of surface silicon that are discussed below. Accordingly, P1 is no more than 1.5, or no more than 1.4, or no more than 1.3, or no more than 1.2, or no more than 1.1, or no more than 1, or no more than 0.95.
For example, P1 may be in the range from 0.55 to 1.4, or from 0.6 to 1.4, or from 0.6 to 1.3, or from 0.65 to 1.3, or from 0.65 to 1.2, or from 0.7 to 1.2, or from 0.7 to 1.1, or from 0.7 to 1, or from 0.75 to 0.95.
As used herein, the micropore volume fraction refers to the volume of micropores expressed as a fraction of the total volume of micropores and mesopores, represented by P1. Put another way, the micropore volume fraction is the volume fraction of pores having diameter of 2 nm or less relative to the total volume of pores having a diameter of up to 50 nm. The micropore volume fraction of the porous framework is preferably selected within the range of 0.43 to 0.85, in order to obtain a high level of surface silicon content in the composite particles (see below).
Preferably, the micropore volume fraction is at least 0.45, or at least 0.48, or at least 0.5, or at least 0.51, or at least 0.52, or at least 0.54, or at least 0.56, or at least 0.58, or at least 0.6 based on the total volume of micropores and mesopores. Preferably, the micropore volume fraction is no more than 0.8, or no more than 0.79, or no more than 0.78, or no more than 0.76, or no more than 0.74, or no more than 0.72, or no more than 0.7, based on the total volume of micropores and mesopores.
The micropore volume fraction may optionally be in the range from 0.45 to 0.85, or from 0.5 to 0.8, or from 0.45 to 0.78, or from 0.48 to 0.8, or from 0.48 to 0.78, or from 0.48 to 0.76, or from 0.5 to 0.8, or from 0.5 to 0.78, or from 0.5 to 0.76, or from 0.5 to 0.74, or from 0.5 to 0.72, or from 0.5 to 0.7, or from 0.51 to 0.76, or from 0.52 to 0.74, or from 0.53 to 0.74, or from 0.54 to 0.72, or from 0.6 to less than 0.8, or from 0.6 to 0.79, or from 0.6 to 0.78, or from 0.6 to 0.76, or from 0.6 to 0.74, or from 0.6 to 0.72, or from 0.6 to 0.7, based on the total volume of micropores and mesopores.
The total volume of micropores and mesopores is determined using nitrogen gas adsorption at 77 K down to a relative pressure p/p0 of 10-6 using quenched solid density functional theory (QSDFT) in accordance with standard methodology as set out in ISO 15901-2 and ISO 15901-3. Nitrogen gas adsorption is a technique that characterizes the porosity of a material by allowing a gas to condense in the pores of a solid. As pressure increases, the gas condenses first in the pores of smallest diameter and the pressure is increased until a saturation point is reached at which all of the pores are filled with liquid. The nitrogen gas pressure is then reduced incrementally, to allow the liquid to evaporate from the system. Analysis of the adsorption and desorption isotherms, and the hysteresis between them, allows the pore volume and pore size distribution to be determined. Suitable instruments for the measurement of pore volume and pore size distributions by nitrogen gas adsorption include the TriStar II and TriStar II Plus porosity analyzers, which are available from Micromeritics Instrument Corporation, USA, and the Autosorb IQ porosity analyzers, which are available from Quantachrome Instruments.
In view of the limitations of available analytical techniques, it is not possible to measure pore volumes across the entire range of micropores, mesopores and macropores using a single technique. In the case that the porous carbon framework comprises macropores, the volume of pores in the range of greater than 50 nm and up to 100 nm is identified herein with the value of P2 cm3/g and is measured by mercury porosimetry. As set out above, the value of P2 relates to the pore volume of the porous carbon framework when measured in isolation, i.e. in the absence of silicon or any other material occupying the pores of the porous carbon framework.
For the avoidance of doubt, the value of p2 takes into account only pores having a diameter of from greater than 50 nm up to and including 100 nm, i.e. it includes only the volume of macropores up to 100 nm in diameter. Any pore volume measured by mercury porosimetry at pore sizes of 50 nm or below is disregarded for the purposes of determining the value of p2 (as set out above, nitrogen adsorption is used to characterize the mesopores and micropores). Pore volume measured by mercury porosimetry above 100 nm is assumed for the purposes of the invention to be inter-particle porosity and is also not take into account when determining the value of P2.
Mercury porosimetry is a technique that characterizes the porosity of a material by applying varying levels of pressure to a sample of the material immersed in mercury. The pressure required to intrude mercury into the pores of the sample is inversely proportional to the size of the pores. Values obtained by mercury porosimetry as reported herein are obtained in accordance with ASTM UOP578-11, with the surface tension γ taken to be 480 mN/m and the contact angle φ taken to be 140° for mercury at room temperature. The density of mercury is taken to be 13.5462 g/cm3 at room temperature. A number of high precision mercury porosimetry instruments are commercially available, such as the AutoPore IV series of automated mercury porosimeters available from Micromeritics Instrument Corporation, USA. For a complete review of mercury porosimetry reference may be made to P.A. Webb and C. Orr in “Analytical Methods in Fine Particle Technology”, 1997, Micromeritics Instrument Corporation, ISBN 0-9656783-0.
The volume of macropores (and therefore the value of P2) is preferably small as compared to the volume of micropores and mesopores (and therefore the value of P1). While a small fraction of macropores may be useful to facilitate electrolyte access into the pore network, the advantages of the invention are obtained substantially by accommodating silicon in micropores and smaller mesopores.
Thus, in accordance with the invention the total volume of macropores in the porous carbon framework is P2 cm3/g as measured by mercury porosimetry, wherein P2 preferably has a value of up to 0.2×P1, or up to 0.1×P1, or up to 0.05×P1, or up to 0.02×P1, or up to 0.01×P1., or up to 0.005×P1.
It will be appreciated that intrusion techniques such as gas adsorption and mercury porosimetry are effective only to determine the pore volume of pores that are accessible to nitrogen or to mercury from the exterior of the porous carbon framework. Porosity values (P1 and P2) as specified herein shall be understood as referring to the volume of open pores, i.e. pores that are accessible to a fluid from the exterior of the porous carbon framework. Fully enclosed pores which cannot be identified by nitrogen adsorption or mercury porosimetry shall not be taken into account herein when specifying porosity values. Likewise, any pore volume located in pores that are so small as to be below the limit of detection by nitrogen adsorption is not taken into account for determining the value of P1.
The porous carbon framework preferably has a BET surface area from 1200 to 3000 m2/g. Preferably the porous carbon framework has a BET surface area of at least 1500 m2/g, or at least 1700 m2/g. Preferably the porous carbon framework has a BET surface area of no more than 2500 m2/g, or no more than 2000 m2/g. The term “BET surface area” as used herein should be taken to refer to the surface area per unit mass calculated from a measurement of the physical adsorption of gas molecules on a solid surface, using the Brunauer-Emmett-Teller theory, in accordance with ISO 9277.
The elemental composition of the composite particles can be determined by elemental analysis. Elemental analysis is used to determine the weight percentages of both silicon and carbon in the composite particles. Optionally, the amounts of hydrogen, nitrogen and oxygen may also be determined by elemental analysis. Preferably, elemental analysis is also used to determine the weight percentage of carbon (and optionally hydrogen, nitrogen and oxygen) in the porous carbon framework alone. Determining the weight percentage of carbon in the in the porous carbon framework alone takes account of the possibility that the porous carbon framework contains a minor amount of heteroatoms within its molecular framework. Both measurements taken together allow the weight percentage of silicon relative to the entire porous carbon framework to be determined reliably.
The silicon content is preferably determined by ICP-OES (Inductively coupled plasma-optical emission spectrometry). A number of ICP-OES instruments are commercially available, such as the iCAP® 7000 series of ICP-OES analyzers available from ThermoFisher Scientific. The carbon content of the composite particles and of the porous carbon framework alone (as well as the hydrogen, nitrogen and oxygen content if required) are preferably determined by combustion and Infrared (IR) absorption techniques. A suitable instrument for determining carbon, hydrogen, nitrogen and oxygen content is the TruSpec® Micro elemental analyzer available from LECO Corporation.
The particulate material of the invention preferably contains from 25 to 65 wt% silicon, more preferably from 30 to 65 wt% silicon, as determined by elemental analysis. Preferably the particulate material of the invention contains at least 26 wt%, or at least 28 wt%, or at least 30 wt%, or at least 32 wt%, or at least 34 wt%, or at least 36 wt%, or at least 38 wt%, or at least 40 wt%, or at least 42 wt%, or at least 44 wt% silicon. Preferably, the particulate material of the invention contains no more than 60 wt%, or no more than 58 wt%, or no more than 56 wt%, or no more than 54 wt%, or no more than 52 wt%, or no more than 50 wt% silicon.
For example, the particulate material of the invention may contain from 26 to 65 wt%, or from 28 to 65 wt%, or from 30 to 65 wt%, or from 32 to 60 wt%, or from 34 to 60 wt%, or from 36 to 60 wt%, or from 38 to 58 wt%, or from 40 to 58 wt%, or from 42 to 56 wt%, or from 44 to 54 wt% silicon.
A minimum amount of silicon is required to ensure that the particulate material has sufficient volumetric capacity for commercial use. However, an excessive amount of silicon results in silicon depositing in larger pores and/or on the surface of the porous carbon framework resulting in a lower content of surface silicon and inferior performance as an electroactive material.
The amount of silicon in the composite particles of the invention is selected such that at least around 20% and up to around 78% of the internal pore volume of the porous carbon framework (based on micropores and mesopores) is occupied by silicon (in the uncharged state). In general, the higher the microporous fraction of the porous carbon framework, the higher the amount of silicon that may be used without reducing the percentage of surface silicon.
Preferably the silicon occupies from about 20% to about 78% of the internal pore volume of the porous carbon framework, for example from about 23% to 75%, or from about 26% to 72%, or from about 28% to 70%, or from about 30% to 70%, or from about 35% to 68%, or from about 40% to 65%, or from about 45 to 60% of the of the internal pore volume of the porous carbon framework. Within these preferred ranges, the pore volume of the porous carbon framework is effective to accommodate expansion of the silicon during charging and discharging, but avoids excess pore volume which does not contribute to the volumetric capacity of the particulate material. However, the amount of silicon is also not so high as to impede effective lithiation due to inadequate metal-ion diffusion rates or due to inadequate expansion volume resulting in mechanical resistance to lithiation.
The amount of silicon in the porous carbon framework can be correlated to the available pore volume by the requirement that the weight ratio of silicon to the porous carbon framework is in the range from [0.50×P1 to 1.9×P1] : 1. This relationship takes into account the density of silicon and the pore volume of the porous carbon framework to define a weight ratio of silicon at which the pore volume is estimated to be around 20% to 78% occupied. Preferably, the weight ratio of silicon to the porous carbon framework is in the range from [0.7×P1 to 1.8×P1] : 1, which indicates that the pore volume is around 30% to 78% occupied.
Preferably, the weight ratio of silicon to the porous carbon framework is at least 0.50×P1, or at least 0.55×P1, or at least 0.6×P1, or at least 0.65×P1, or 0.7×P1, or at least 0.75×P1, or at least 0.8×P1, or at least 0.85×P1, or at least 0.9×P1, or at least 0.95×P1, or at least 1×1. Preferably, the weight ratio of silicon to the porous carbon framework is no more than 1.85×P1, or no more than 1.8×P1, or no more than 1.75×P1, or no more than 1.7×P1, or no more than 1.65×P1, or no more than 1.6×P1, or no more than 1.55×P1, or no more than 1.5×P1.
The composite particles preferably have a low total oxygen content, as determined by elemental analysis. Oxygen may be present in the composite particles for instance as part of the porous carbon framework or as an oxide layer on any exposed silicon surfaces. Preferably, the total oxygen content of the composite particles is less than 15 wt%, more preferably less than 12 wt%, more preferably less than 10 wt%, more preferably less than 5 wt%, for example less than 4 wt%, or less than 3 wt%, or less than 2 wt%, or less than 1 wt%, or less than 0.5 wt%. Preferably silicon and carbon together constitute at least 90 wt% of the composite particles, more preferably at least 95 wt% of the composite particles.
The silicon may optionally comprise a minor amount of one or more dopants. Suitable dopants include boron and phosphorus, other n-type or p-type dopants, nitrogen, or germanium. Preferably, the dopants are present in a total amount of no more than 2 wt% based on the total amount of silicon and the dopant(s).
Atoms at the surface of a material have different set of bonding interactions to atoms in the bulk of the material, and this difference is usually described in terms of the surface energy of the material. In the case of silicon that has been deposited by chemical vapor infiltration (CVI), the free valencies of silicon atoms at the surface generally carry hydride groups. If this hydride-terminated silicon surface is accessible to air, it reacts with oxygen to form a native oxide surface. However, surfaces that are not accessible to air remain in the hydride-terminated form. The amount of this surface silicon can be quantified using thermogravimetric analysis (TGA). Silicon atoms at the surface of a silicon nanostructure are oxidized at a lower temperature than silicon atoms in the bulk of a silicon nanostructure (reference: Bardet et al., Phys. Chem. Chem. Phys. (2016), 18, 18201). TGA analysis allows for the relative content of surface silicon to be quantified, based on the weight gain that is observed as silicon is oxidized to silicon dioxide (SiO2) in air and at elevated temperature. By plotting the weight gain against temperature it is possible to differentiate and quantify the bulk and surface silicon in the sample.
The determination of the amount of unoxidized surface silicon is derived from the characteristic TGA trace for these materials, as shown in
Any native oxide that is already formed on silicon surfaces that are exposed to air does not affect the TGA analysis, since silicon that is already oxidized does not give rise to a mass increase in the TGA analysis. Therefore the more the silicon surfaces are able to react with air to form a native oxide, the less surface silicon is observed by TGA. For avoidance of doubt, the calculation of “surface silicon” therefore takes into account only silicon which is unoxidized at the start of the TGA analysis after the material has been passivated by air or another surface passivating agent as described herein (i.e. the particulate material is not kept under any special inert conditions prior to the TGA analysis).
As defined herein, “surface silicon” is calculated from the initial mass increase in the TGA trace from a minimum between 150° C. and 500° C. to the maximum mass measured in the temperature range between 550° C. and 650° C., wherein the TGA is carried out in air with a temperature ramp rate of 10° C./min. This mass increase is assumed to result from the oxidation of surface silicon and therefore allows the percentage of surface silicon as a proportion of the total amount of silicon to be determined according to the following formula:
Wherein Y is the percentage of surface silicon as a proportion of the total silicon in the sample, Mmax is the maximum mass of the sample measured in the temperature range between 550° C. to 650° C. (mass (c) in
It has been found that reversible capacity retention over multiple charge/discharge cycles is considerably improved when the surface silicon as determined by the TGA method described above is at least 20 wt% of the total amount of silicon in the material. Preferably at least 22 wt%, or at least 25 wt%, at least 30 wt% of the silicon, or at least 35 wt% of the silicon, or at least 40 wt% of the silicon, or at least 45 wt% of the silicon is surface silicon as determined by thermogravimetric analysis (TGA).
Optionally, the amount of surface silicon as determined by TGA is up to 80 wt%, or up to 75 wt%, or up to 70 wt%, or up to 65 wt%, or up to 60 wt%, or up to 55 wt% of the total amount of silicon in the particulate material. For example, the amount of surface silicon as determined by TGA may be from 20 to 80 wt%, or from 22 to 75 wt%, or from 25 to 70 wt%, or from 30 to 65 wt%, or from 35 to 60 wt%, or from 40 to 55 wt% of the total amount of silicon in the particulate material. The amount of surface silicon as determined by TGA may also be in the range from 20 to 55 wt%, or from 22 to 60 wt%, or from 25 to 65 wt%, or from 30 to 70 wt%, or from 35 to 75 wt%, or from 40 to 80 wt% of the total amount of silicon in the particulate material. Further preferred ranges may be defined by combining the upper and lower limits of any of the aforementioned ranges.
The fact that a significant proportion of hydride-terminated surface silicon is measurable in the particulate material even after passivation in air indicates that the composite particles contain internal silicon surfaces that are inaccessible to air. This indicates that the internal pore spaces of the porous carbon framework are first lined with silicon before being capped to form an internal void space with the hydride-terminated silicon surfaces oriented into the closed internal void space. This in turn indicates that the silicon domains have a characteristic length scale that is much smaller that the pores themselves.
As the internal voids are inaccessible to electrolyte, the silicon surfaces are protected from SEI formation, thereby minimising irreversible lithium loss during the first charge cycle. Additional exposure of the electroactive material in subsequent charge-discharge cycles is also substantially prevented such that SEI formation is not a significant failure mechanism leading to capacity loss. Simultaneously, this silicon is constrained hydrostatically during lithiation enabling utilization of the voids during lithiation induced expansion.
In addition to the surface silicon content, the particulate material of the invention preferably has a low content of coarse bulk silicon as determined by TGA. Coarse bulk silicon is defined herein as silicon which undergoes oxidation above 800° C. as determined by TGA, wherein the TGA is carried out in air with a temperature ramp rate of 10° C./min. This is shown in
Wherein Z is the percentage of unoxidized silicon at 800° C., M800 is the mass of the sample at 800° C. (mass (d) in
Preferably, no more than 10 wt% of the silicon, or no more than 8 wt% of the silicon, or no more than 6 wt% of the silicon, or no more than 5 wt%, or no more than 4 wt%, or no more than 3 wt%, or no more than 2 wt% or no more than 1.5 wt% of the silicon is coarse bulk silicon as determined by TGA.
Preferably at least 30 wt% of the silicon (for example 30 to 75 wt%, 30 to 70 wt% or 30 to 65 wt% of the silicon) is surface silicon and no more than 10 wt% of the silicon is coarse bulk silicon, wherein both are determined by TGA. More preferably at least 35 wt% of the silicon (for example 35 to 70 wt%, 35 to 65 wt% or 35 to 60 wt% of the silicon) is surface silicon and no more than 8 wt% of the silicon is coarse bulk silicon, wherein both are determined by TGA. More preferably, at least 40 wt% of the silicon (for example 40 to 65 wt%, 40 to 60 wt%, or 40 to 55 wt% of the silicon) is surface silicon and no more than 5 wt% of the silicon is coarse bulk silicon, wherein both are determined by TGA. More preferably, at least 45 wt% of the silicon (for example 45 to 65 wt%, 45 to 60 wt%, or 45 to 55 wt% of the silicon) is surface silicon and no more than 2 wt% of the silicon is coarse bulk silicon, wherein both are determined by TGA.
Preferably, the total volume of micropores and mesopores in the composite particles (i.e. in the presence of the silicon), as measured by nitrogen gas adsorption, is up to 0.15 × P1, or up to 0.10 × P1, or up to 0.05 × P1, or up to 0.02 × P1.
Preferably the total volume of micropores and mesopores in the composite particles, as measured by nitrogen gas adsorption, is less than 0.2 cm3/g, preferably less than 0.15 cm3/g, or less than 0.1 cm3/g, or less than 0.08 cm3/g, or less than 0.06 cm3/g, or less than 0.04 cm3/g, or less than 0.02 cm3/g, or less than 0.015 cm3/g, or less than 0.012 cm3/g, or less than 0.010 cm3/g, or less than 0.008 cm3/g.
The composite particles may have a D50 particle diameter in the range from 1 to 30 µm. Optionally, the D50 particle diameter may be at least 1 µm, or at least 2 µm, or at least 3 µm, or at least 4 µm, or at least 5 µm. Optionally the D50 particle diameter may be no more than 20 µm, or no more than 18 µm, or no more than 16 µm, or no more than 14 µm, or no more than 12 µm, or no more than 10 µm, or no more than 8 µm.
For instance, the composite particles may have a D50 particle diameter in the range from 1 to 20 µm, or from 1 to 18 µm, or from 1 to 16 µm, or from 2 to 16 µm, or from 2 to 14 µm, or from 2 to 12 µm, or from 2 to 10 µm, or from 2 to 8 µm. Particles within these size ranges and having porosity and a pore diameter distribution as set out herein are ideally suited for use in anodes for metal-ion batteries, due to their dispersibility in slurries, their structural robustness, their capacity retention over repeated charge-discharge cycles, and their suitability for forming dense electrode layers of uniform thickness in the conventional range from 20 to 50 µm.
The D10 particle diameter of the composite particles is preferably at least 0.5 µm, or at least 0.8 µm, or at least 1 µm. By maintaining the D10 particle diameter at 0.5 µm or more, the potential for undesirable agglomeration of sub-micron sized particles is reduced, resulting in improved dispersibility of the particulate material and improved capacity retention.
The D90 particle diameter of the composite particles is preferably no more than 50 µm, or no more than 40 µm, or no more than 30 µm, or no more than 25 µm, or no more than 20 µm, or no more than 15 µm. The presence of very large particles results in non-uniform forming packing of the particles in electrode active layers, thus disrupting the formation of dense electrode layers, particularly electrode layers having a thickness in the range from 20 to 50 µm. Therefore, it is preferred that the D90 particle diameter is up to 40 µm, and more preferably lower still.
The composite particles preferably have a narrow size distribution span. For instance, the particle size distribution span (defined as (D90-D10)/D50) is preferably 5 or less, more preferably 4 or less, more preferably 3 or less, more preferably 2 or less, and most preferably 1.5 or less. By maintaining a narrow size distribution span, efficient packing of the particles into dense electrode layers is more readily achievable.
The composite particles preferably have a positive skew in the volume-based distribution, for example, such that the volume based distribution is asymmetric with a longer tail on the right hand side. A positive skew in the volume-based particle size distribution is advantageous since it provides a denser electrode since the natural packing factor will be higher than if all particles are the same size, thereby reducing the need for calendering or other physical densification processes. Preferably, the D50 composite particle size diameter is less than the volume-based mean of the particle size diameter distribution (D[4.3]). Preferably, the skew of the composite particle size distribution (as measured by a Malvern Mastersizer™ 3000 analyzer) is no more than 5, or no more than 3.
The composite particles of the invention preferably have a BET surface area of no more than 200 m2/g. Preferably, the BET surface area of the composite particles is no more than 150 m2/g, or no more than 100 m2/g, or no more than 80 m2/g, or no more than 60 m2/g, or no more than 50 m2/g, or no more than 40 m2/g, or no more than 30 m2/g, or no more than 25 m2/g, or no more than 20 m2/g, or no more than 15 m2/g, or no more than 10 m2/g.
In general, a low BET surface area is preferred in order to minimize the formation of solid electrolyte interphase (SEI) layers at the surface of the composite particles during the first charge-discharge cycle of an anode comprising the particulate material of the invention. However, a BET surface area which is excessively low results in unacceptably low charging rate and capacity limitations due to the inaccessibility of the bulk of the electroactive material to metal ions in the surrounding electrolyte. For instance, the BET surface area is preferably at least 0.1 m2/g, or at least 1 m2/g, or at least 2 m2/g, or at least 5 m2/g. For instance, the BET surface area may be in the range from 1 m2/g to 25 m2/g, more preferably in the range from 2 to 15 m2/g.
The particulate material of the invention typically has a specific charge capacity on first lithiation of 900 to 2300 mAh/g. Preferably, the particulate material of the invention has a specific charge capacity on first lithiation of at least 1200 mAh/g, or at least 1400 mAh/g.
The particulate material of the invention may optionally comprise a silicon surface that has been treated with a passivating agent. As discussed in further detail below, a passivating agent is defined herein as a compound that is capable of modifying the surface of the electroactive material in such a way as to inhibit or prevent the formation of surface oxides.
The composite particles of the invention may optionally include a coating that at least partially or fully covers the external surfaces of the particles. The coating is preferably a lithium-ion permeable coating. As used herein, the term “lithium ion permeable” refers to an ionically conductive material that allows the transport of lithium ions from the exterior of the composite particles to the nanoscale electroactive material domains. Preferably, the lithium-ion permeable coating is impermeable to liquids, such as the solvents of liquid electrolytes. Preferably, the lithium-ion permeable filler material is electrochemically stable at < 0.1 V vs. Li/Li+.
Optionally the coating may comprise a conductive carbon coating. Suitably a conductive carbon coating may be obtained by a chemical vapour deposition (CVD) method. CVD is a well-known methodology in the art and comprises the thermal decomposition of a volatile carbon-containing gas (e.g. ethylene) onto the surface of the particulate material. Alternatively, the carbon coating may be formed by depositing a solution of a carbon-containing compound onto the surface of the particulate material followed by pyrolysis. The conductive carbon coating is sufficiently permeable to allow lithium access to the interior of the composite particles without excessive resistance, so as not to reduce the rate performance of the composite particles. For instance, the thickness of the carbon coating may be in the range from 2 to 30 nm. Optionally, the carbon coating may be porous and/or may only cover partially the surface of the composite particles.
Alternatively, the coating may comprise a lithium-ion permeable solid electrolyte. Examples of suitable lithium permeable solid electrolytes include: garnet-type solid electrolytes (including “LLZO” electrolytes such as Li7La3Zr2O12 and Li6.5La3Ti0.5Zr1.5O12); perovskite-type solid electrolytes (including “LLTO” electrolytes such as Li0.33La0.57TiO3); LISICON-type solid electrolytes, NaSICON-type solid electrolytes (such as Li1.3Al0.3Ti1.7(PO4)3); lithium phosphorous oxy-nitride (LiPON) solid electrolytes; Li3N-type solid electrolytes; lithium phosphate (Li3PO4) solid electrolytes, lithium titanate (Li4Ti5O12) solid electrolytes; lithium tantalate (LiTaO3) solid electrolytes; sulfide-type solid electrolytes; argyrodite-type solid electrolytes; and anti-perovskite-type solid electrolytes. Variants (e.g. including dopants) and combinations of these electrolyte types are also included.
A coating has the advantages that it further reduces the BET surface area of the particulate material by smoothing any surface defects and by filling any remaining surface microporosity, thereby further reducing first cycle loss. The use of electronically conductive coatings, such as a carbon coating, is particularly advantageous as it improves the conductivity of the surface of the composite particles, improving the rate performance of the particulate material when used as electroactive materials in lithium-ion batteries, and/or reducing the need for conductive additives in electrode compositions, and also creates an improved surface for the formation of a stable SEI layer, resulting in improved capacity retention on cycling. In the case that the composite particles comprise a coating, the silicon content of the particles in wt% is determined based on the weight of the particles including the coating.
The composite particles of the invention are suitably prepared via chemical vapor infiltration (CVI) of a silicon-containing precursor into the pore structure of the porous carbon framework. As used herein, CVI refers to processes in which a gaseous silicon-containing precursor is thermally decomposed on a surface to form elemental silicon at the surface and gaseous by-products.
According to a second aspect of the invention, there is provided a particulate material comprising a plurality of composite particles, wherein the composite particles comprise:
The particulate material of the second aspect of the invention may have any of the features described as preferred or optional with regard to the first aspect of the invention.
In a third aspect of the invention, there is provided a composition comprising a particulate material according to the first aspect or second aspect of the invention and at least one other component. In particular, there is provided a composition comprising a particulate material according to the first aspect of the invention and at least one other component selected from: (i) a binder; (ii) a conductive additive; and (iii) an additional particulate electroactive material. The composition according to the third aspect of the invention is useful as an electrode composition, and thus may be used to form the active layer of an electrode.
The particulate material used to prepare the composition of the third aspect of the invention may have any of the features described as preferred or optional with regard to the first and second aspects of the invention.
The composition may be a hybrid electrode composition which comprises a particulate material according to the first aspect of the invention and at least one additional particulate electroactive material. Examples of additional particulate electroactive materials include graphite, hard carbon, silicon, tin, germanium, aluminium and lead. The at least one additional particulate electroactive material is preferably selected from graphite and hard carbon, and most preferably the at least one additional particulate electroactive material is graphite.
In the case of a hybrid electrode composition, the composition preferably comprises from 3 to 60 wt%, or from 3 to 50 wt%, or from 5 to 50 wt%, or from 10 to 50 wt%, or from 15 to 50 wt%, of the particulate material according to the first aspect of the invention, based on the total dry weight of the composition.
The at least one additional particulate electroactive material is suitably present in an amount of from 20 to 95 wt%, or from 25 to 90 wt%, or from 30 to 750 wt% of the at least one additional particulate electroactive material.
The at least one additional particulate electroactive material preferably has a D50 particle diameter in the range from 10 to 50 µm, preferably from 10 to 40 µm, more preferably from 10 to 30 µm and most preferably from 10 to 25 µm, for example from 15 to 25 µm.
The D10 particle diameter of the at least one additional particulate electroactive material is preferably at least 5 µm, more preferably at least 6 µm, more preferably at least 7 µm, more preferably at least 8 µm, more preferably at least 9 µm, and still more preferably at least 10 µm.
The D90 particle diameter of the at least one additional particulate electroactive material is preferably up to 100 µm, more preferably up to 80 µm, more preferably up to 60 µm, more preferably up to 50 µm, and most preferably up to 40 µm.
The at least one additional particulate electroactive material is preferably selected from carbon-comprising particles, graphite particles and/or hard carbon particles, wherein the graphite and hard carbon particles have a D50 particle diameter in the range from 10 to 50 µm. Still more preferably, the at least one additional particulate electroactive material is selected from graphite particles, wherein the graphite particles have a D50 particle diameter in the range from 10 to 50 µm.
The composition may also be a non-hybrid (or “high loading”) electrode composition which is substantially free of additional particulate electroactive materials. In this context, the term “substantially free of additional particulate electroactive materials” should be interpreted as meaning that the composition comprises less than 15 wt%, preferably less than 10 wt%, preferably less than 5 wt%, preferably less than 2 wt%, more preferably less than 1 wt%, more preferably less than 0.5 wt% of any additional electroactive materials (i.e. additional materials which are capable of inserting and releasing metal ions during the charging and discharging of a battery), based on the total dry weight of the composition.
A “high-loading” electrode composition of this type preferably comprises at least 50 wt%, or at least 60 wt%, or at least 70 wt%, or at least 80 wt%, or at least 90 wt% of the particulate material according to the first aspect of the invention, based on the total dry weight of the composition.
The composition may optionally comprise a binder. A binder functions to adhere the composition to a current collector and to maintain the integrity of the composition. Examples of binders which may be used in accordance with the present invention include polyvinylidene fluoride (PVDF), polyacrylic acid (PAA) and alkali metal salts thereof, modified polyacrylic acid (mPAA) and alkali metal salts thereof, carboxymethylcellulose (CMC), modified carboxymethylcellulose (mCMC), sodium carboxymethylcellulose (Na-CMC), polyvinylalcohol (PVA), alginates and alkali metal salts thereof, styrene-butadiene rubber (SBR) and polyimide. The composition may comprise a mixture of binders. Preferably, the binder comprises polymers selected from polyacrylic acid (PAA) and alkali metal salts thereof, and modified polyacrylic acid (mPAA) and alkali metal salts thereof, SBR and CMC.
The binder may suitably be present in an amount of from 0.5 to 20 wt%, preferably 1 to 15 wt%, preferably 2 to 10 wt% and most preferably 5 to 10 wt%, based on the total dry weight of the composition.
The binder may optionally be present in combination with one or more additives that modify the properties of the binder, such as cross-linking accelerators, coupling agents and/or adhesive accelerators.
The composition may optionally comprise one or more conductive additives. Preferred conductive additives are non-electroactive materials that are included so as to improve electrical conductivity between the electroactive components of the composition and between the electroactive components of the composition and a current collector. The conductive additives may be selected from carbon black, carbon fibers, carbon nanotubes, graphene, acetylene black, ketjen black, metal fibers, metal powders and conductive metal oxides. Preferred conductive additives include carbon black and carbon nanotubes.
The one or more conductive additives may suitably be present in a total amount of from 0.5 to 20 wt%, preferably 1 to 15 wt%, preferably 2 to 10 wt% and most preferably 5 to 10 wt%, based on the total dry weight of the composition.
In a fourth aspect, the invention provides an electrode comprising a particulate material as defined with reference to the first or second aspects of the invention in electrical contact with a current collector. The particulate material used to prepare the electrode of the fourth aspect of the invention may have any of the features described as preferred or optional with regard to the first and second aspects of the invention.
As used herein, the term current collector refers to any conductive substrate that is capable of carrying a current to and from the electroactive particles in the composition. Examples of materials that can be used as the current collector include copper, aluminium, stainless steel, nickel, titanium and sintered carbon. Copper is a preferred material. The current collector is typically in the form of a foil or mesh having a thickness of between 3 to 500 µm. The particulate materials of the invention may be applied to one or both surfaces of the current collector to a thickness which is preferably in the range from 10 µm to 1 mm, for example from 20 to 500 µm, or from 50 to 200 µm.
Preferably, the electrode comprises a composition as defined with reference to the third aspect of the invention in electrical contact with a current collector. The composition may have any of the features described as preferred or optional with regard to the third aspect of the invention.
The electrode of the fourth aspect of the invention may be fabricated by combining the particulate material of the invention (optionally in the form of the composition of the invention) with a solvent and optionally one or more viscosity modifying additives to form a slurry. The slurry is then cast onto the surface of a current collector and the solvent is removed, thereby forming an electrode layer on the surface of the current collector. Further steps, such as heat treatment to cure any binders and/or calendaring of the electrode layer may be carried out as appropriate. The electrode layer suitably has a thickness in the range from 20 µm to 2 mm, preferably 20 µm to 1 mm, preferably 20 µm to 500 µm, preferably 20 µm to 200 µm, preferably 20 µm to 100 µm, preferably 20 µm to 50 µm.
Alternatively, the slurry may be formed into a freestanding film or mat comprising the particulate material of the invention, for instance by casting the slurry onto a suitable casting template, removing the solvent and then removing the casting template. The resulting film or mat is in the form of a cohesive, freestanding mass that may then be bonded to a current collector by known methods.
The electrode of the fourth aspect of the invention may be used as the anode of a metal-ion battery. Thus, in a fifth aspect, the present invention provides a rechargeable metal-ion battery comprising an anode, the anode comprising an electrode as described above, a cathode comprising a cathode active material capable of releasing and reabsorbing metal ions; and an electrolyte between the anode and the cathode.
The metal ions are preferably lithium ions. More preferably, the rechargeable metal-ion battery of the invention is a lithium-ion battery, and the cathode active material is capable of releasing and accepting lithium ions.
The cathode active material is preferably a metal oxide-based composite. Examples of suitable cathode active materials include LiCoO2, LiCo0.99Al0.01O2, LiMiO2, LiMnO2, LiCo0.5Ni0.5O2, LiCo0.7Ni0.3O2, LiCo0.8Ni0.2O2, LiCo0.82Ni0.18O2, LiCO0.8Ni0.15Al0.05O2, LiNi0.4Co0.3Mn0.3O2 and LiNi0.33Co0.33Mn0.34O2. The cathode current collector is generally of a thickness of between 3 to 500 µm. Examples of materials that can be used as the cathode current collector include aluminium, stainless steel, nickel, titanium and sintered carbon.
The electrolyte is suitably a non-aqueous electrolyte containing a metal salt, e.g. a lithium salt, and may include, without limitation, non-aqueous electrolytic solutions, solid electrolytes and inorganic solid electrolytes. Examples of non-aqueous electrolyte solutions that can be used include non-protic organic solvents such as propylene carbonate, ethylene carbonate, butylene carbonates, dimethyl carbonate, diethyl carbonate, gamma butyrolactone, 1,2-dimethoxyethane, 2-methyltetrahydrofuran, dimethylsulfoxide, 1,3-dioxolane, formamide, dimethylformamide, acetonitrile, nitromethane, methylformate, methyl acetate, phosphoric acid triesters, trimethoxymethane, sulfolane, methyl sulfolane and 1,3-dimethyl-2-imidazolidinone.
Examples of organic solid electrolytes include polyethylene derivatives polyethyleneoxide derivatives, polypropylene oxide derivatives, phosphoric acid ester polymers, polyester sulfide, polyvinylalcohols, polyvinylidine fluoride and polymers containing ionic dissociation groups.
Examples of inorganic solid electrolytes include nitrides, halides and sulfides of lithium salts such as Li5Nl2, Li3N, Lil, LiSiO4, Li2SiS3, Li4SiO4, LiOH and Li3PO4.
The lithium salt is suitably soluble in the chosen solvent or mixture of solvents. Examples of suitable lithium salts include LiCl, LiBr, Lil, LiClO4, LiBF4, LiBC4O8, LiPF6, LiCF3SO3, LiAsF6, LiSbF6, LiAlCl4, CH3SO3Li and CF3SO3Li.
Where the electrolyte is a non-aqueous organic solution, the metal-ion battery is preferably provided with a separator interposed between the anode and the cathode. The separator is typically formed of an insulating material having high ion permeability and high mechanical strength. The separator typically has a pore diameter of between 0.01 and 100 µm and a thickness of between 5 and 300 µm. Examples of suitable electrode separators include a micro-porous polyethylene film.
The separator may be replaced by a polymer electrolyte material and in such cases the polymer electrolyte material is present within both the composite anode layer and the composite cathode layer. The polymer electrolyte material can be a solid polymer electrolyte or a gel-type polymer electrolyte.
According to a sixth aspect of the invention, there is provided a process for preparing a particulate material according to the first aspect of the invention, the process comprising the steps of:
According to a seventh aspect of the invention, there is provided a process for preparing a particulate material according to the first aspect of the invention, the process comprising the steps of:
The particulate material prepared according to the sixth and seventh aspects of the invention may have any of the features described above as preferred or optional with regard to the first aspect of the invention. In particular, the porous carbon particles may have any of the features of the porous carbon frameworks described in relation to the first aspect of the invention. In particular, the porous carbon particles are preferably steam-activated.
According to an eighth aspect of the invention, there is provided a process for preparing a particulate material according to the second aspect of the invention, the process comprising the steps of:
The particulate material prepared according to the eighth aspect of the invention may have any of the features described above as preferred or optional with regard to the second aspect of the invention. The porous carbon particles may have any of the features of the porous carbon frameworks described in relation to the first aspect of the invention. In particular, the porous carbon particles are preferably steam-activated.
The following preferred features apply to all of the sixth, seventh and eighth aspects, unless indicated otherwise.
Suitable gaseous silicon-containing precursors for use in the sixth to eighth aspects of the invention include silane (SiH4), silane derivatives (e.g. disilane, trisilane and tetrasilane), and trichlorosilane (SiHCl3).
Optionally, the silicon-containing precursor is free of chlorine. Free of chlorine means that the silicon-containing precursor contains less than 1 wt%, preferably less than 0.1 wt%, preferably less than 0.01 wt% of chlorine-containing compounds.
The silicon-containing precursors may be used either in pure form or more usually as a diluted mixture with an inert carrier gas, such as nitrogen or argon.
Step (b) is suitably carried out at low partial pressure of silicon precursor with total pressure of 101.3 kPa (i.e. 1 atm) or below, the remaining partial pressure using an inert padding gas such as hydrogen, nitrogen or argon.
In accordance with the sixth and eighth aspects of the invention, the silicon-containing precursor is used in an amount in the range from 0.5 to 20 vol%, for instance from 1 to 10 vol%, or 1 to 5 vol%, preferably at least 3 vol%, based on the total volume of the silicon-containing precursor and the inert carrier gas.
In accordance with the seventh aspect of the invention, the partial pressure of the silicon-containing precursor is from 0.5 to 20 kPa, or from 1 to 15 kPa, or from 1 to 10 kPa, or from 1 to 5 kPa. As used herein, the partial pressure of the silicon precursor gas is defined as the total pressure multiplied by the volume fraction of the silicon precursor gas (i.e. assuming ideal gas behaviour). If the silicon precursor gas is used neat, then the partial pressure of the silicon precursor gas equals the total pressure. Alternatively, the total pressure may be the sum of the partial pressures of the silicon precursor gas and an inert padding gas, such as nitrogen or argon.
Temperatures ranging from 400-700° C. are used in step (b), preferably from 425-550° C., or 425-500° C. Optionally, the porous carbon particles are contacted with the silicon precursor gas at an initial temperature of less than 400° C. and the reaction temperature is then increased into the range from 400-700° C.
Step (b) is optionally preferably performed with agitation or fluidization of the porous carbon particles, this is particularly preferred when the process is carried out on a large scale. Suitable reactor types include a rotary kiln, or fluidized bed reactor (including spouted bed reactor).
In order to obtain the particulate material of the invention with a high content of surface silicon, it is necessary that the CVI process be carefully controlled to ensure that the rate of silicon deposition is low relative to the rate of diffusion of the silicon precursor gas into the pore structure of the porous carbon framework. Operation in the preferred temperature range of 425-500° C. and the use of a low concentration of the silicon precursor gas can also control the rate of silicon deposition, ensuring that the rate of silicon deposition is low relative to the infiltration rate of the silicon precursor. The conditions within the CVI reactor should also be as homogenous as possible. Agitation or fluidization of the porous carbon particles ensures that the silicon precursor gas is able to infiltrate the particles uniformly and also ensures that the temperature in the reactor is homogenous throughout the particle bed.
Preferably, step (b) is carried out at a pressure below atmospheric pressure. For example, step (b) can be carried out at an absolute pressure of less than 100 kPa, or less than 90 kPa, or less than 80 kPa, or less than 70 kPa, or less than 60 kPa. Preferably, step (b) is carried out at an absolute pressure of at least 5 kPa, or at least 10 kPa, or at least 15 kPa, or at least 20 kPa, or at least 25 kPa, or at least 30 kPa. For example, step b is preferably carried out at an absolute pressure in the range from 10 to 90 kPa, or from 20 to 80 kPa, or from 20 to 70 kPa, or from 30 to 60 kPa.
It has been found that carrying out step (b) at an absolute pressure below atmospheric pressure results in a significant improvement in the surface silicon content of the particulate material product.
Preferred operating conditions in step (b) for forming a particulate material product comprising over 20% surface silicon include the use of a gas comprising 0.5 to 20 vol% of a silicon precursor gas (preferably silane), at an absolute pressure of 10 to 90 kPa. More preferably, a gas comprising 2 to 15 vol% of a silicon precursor is used at an absolute pressure of 20 to 80 kPa. More preferably, a gas comprising 5 to 10 vol% of a silicon precursor is used at an absolute pressure of 30 to 60 kPa. With reference to the appended examples, operation within these preferred conditions reliably provides a particulate material with a very high surface silicon content of at least 30% or even at least 40%. Careful selection of the porous carbon particles together with the use of the controlled CVI conditions described herein allows a particulate material to be obtained with a very high content of surface silicon and a low content of coarse bulk silicon, indicating that a high proportion of the silicon is present in the form of ultrafine silicon nanostructures. Such materials have not been reported in the art previously.
The surfaces of electroactive materials deposited by CVI are reactive to oxygen and form a native oxide layer when exposed to atmospheric oxygen. In the case of silicon, an amorphous silicon dioxide film is formed immediately when a silicon surface is exposed to oxygen and in certain circumstances oxidation can continue with prolonged exposure during storage. The formation of the native oxide layer is exothermic and therefore requires careful process control to prevent overheating or even combustion of the particulate material during manufacture or storage. The presence of a native oxide layer is associated with irreversible capacity loss and reduced cycle life, and so may be deleterious to the performance of the electroactive materials in lithium-ion batteries. Therefore, the process of the invention may optionally comprise the additional step (c) of contacting the exposed surfaces of the deposited silicon with a passivating agent, wherein the silicon is not exposed to oxygen prior to contact with the passivating agent.
A passivating agent is defined herein as a compound that is capable of modifying the surface of the electroactive material in such a way as to inhibit or prevent the formation of surface oxides.
Suitable passivating agents include compounds comprising an alkene, alkyne or carbonyl functional group, more preferably a terminal alkene, terminal alkyne or aldehyde group.
Preferred passivating agents include one or more compounds of the formulae:
wherein R represents H or an unsubstituted or substituted aliphatic or aromatic hydrocarbyl group having from 1 to 20 carbon atoms, preferably from 2 to 10 carbon atoms, or whereintwo R groups in formula (i) form an unsubstituted or substituted hydrocarbyl ring structure comprising from 3 to 8 carbon atoms.
Particularly preferred passivating agents include one or more compounds of the formulae:
wherein R is as defined above. Preferably, R is unsubstituted.
Examples of suitable compounds include ethylene, propylene, 1-butene, butadiene, 1-pentene, 1,4-pentadiene, 1-hexene, 1-octene, styrene, divinylbenzene, acetylene, phenylacetylene, norbornene, norbornadiene and bicyclo[2.2.2]oct-2-ene. Mixtures of different passivating agents may also be used. A preferred passivating agent is ethylene
It is believed that the alkene, alkyne or carbonyl group of the passivating agent undergoes an insertion reaction with M-H groups at the surface of the electroactive material (where M represents an atom of the electroactive material) to form a covalently passivated surface which is resistant to oxidation by air. When silicon is the electroactive material, the passivation reaction between the silicon surface and the passivating agent may be understood as a form of hydrosilylation, as shown schematically below.
Other suitable passivating agents include compounds including an active hydrogen atom bonded to oxygen, nitrogen, sulphur or phosphorus. For example, the passivating agent may be an alcohol, amine, thiol or phosphine. Reaction of the group -XH with hydride groups at the surface of the electroactive material is understood to result in elimination of H2 and the formation of a direct bond between X and the electroactive material surface.
Suitable passivating agents in this category include compounds of the formula:
wherein X represents O, S, NR or PR, and wherein each R is independently as defined above. Two R groups in formula (iv) may also form an unsubstituted or substitutedhydrocarbyl ring structure comprising from 3 to 8 carbon atoms. Preferably X represents O or NH and R represents an optionally substituted aliphatic or aromatic group having from 2 to 10 carbon atoms. Amine groups may also be incorporated into a 4-10 membered aliphatic or aromatic ring structure, as in pyrrolidine, pyrrole, imidazole, piperazine, indole, or purine.
Where the passivating agent is a carbon-containing compound, contacting of the electroactive material with the passivating agent in step (c) may be carried out above or below the pyrolysis temperature of the passivating agent. When the electroactive material is contacted with the passivating agent below the pyrolysis temperature of the passivating agent, a passivation layer only is formed on the silicon surface. When the electroactive material is contacted with the passivating agent above the pyrolysis temperature of the passivating agent, passivation of the silicon surface occurs together with the formation of a pyrolytic carbon coating
Contacting of the electroactive material with the passivating agent in step (c) may be carried out at a temperature in the range of 25 to 700° C. and at pressures in the range from 100 kPa to 50 MPa. For example, step (c) may suitably be carried out within the preferred temperature and pressure ranges for step (b) as set out herein.
A further suitable passivating agent is ammonia. Step (c) may therefore comprise contacting the surface of the deposited electroactive material with ammonia at a temperature in the range of from 200-700° C., preferably from 400-700° C. For example, where the passivating agent is ammonia, step (c) may be carried out at the same temperature as is used to deposit the electroactive material in step (b). The temperature is then increased if necessary into the range of 500 to 1,000° C. to form a crystalline nitride surface (e.g. a silicon nitride surface of the formula SiNx, wherein x ≤4/3). Passivation with ammonia therefore provides an alternative means to limit oxidation of the electroactive material. As sub-stoichiometric silicon nitride is conductive, this step will also result in the formation of a conductive network that will allow for faster charging and discharge of the electroactive material.
The passivation in step (c) may optionally be carried out in the same reactor as step (b), for example by stopping the flow of the silicon precursor gas to the reactor and starting the flow of a passivating agent gas to the reactor. Optionally, the reactor may be flushed with an inert gas prior to step (c).
The process of the invention may optionally comprise the additional step (d) of forming a conductive carbon coating on the surfaces of the composite particles from step (b), or from step (c) if a passivation step is carried out. Step (d) suitably comprises contacting the electroactive material with a pyrolytic carbon precursor at a temperature above the pyrolysis temperature of the pyrolytic carbon precursor.
Suitable conditions for step (d) are discussed in detail in WO 2021/048556.
As an example of a fixed-bed reactor method (experimental scale), 1.8 g of a particulate porous carbon framework was placed on a stainless-steel plate at a constant thickness of 1 mm along its length. The plate was then placed inside a stainless-steel tube of outer diameter 60 mm with gas inlet and outlet lines located in the hot zone of a retort furnace. The furnace tube was purged with nitrogen gas for 30 minutes at room temperature, then the sample temperature was increased to 450-500° C. The nitrogen gas flow-rate is adjusted to ensure a gas residence time of at least 90 seconds in the furnace tube and maintained at that rate for 30 minutes. Then, the gas supply is switched from nitrogen to a mixture of monosilane in nitrogen at 1.25 vol. % concentration. Dosing of monosilane is performed over a 5-hour period with a reactor pressure maintained at 101.3 kPa (1 atm). After dosing has finished the gas flow rate is kept constant whilst the silane is purged from the furnace using nitrogen. The furnace is purged for 30 minutes under nitrogen. Optionally, a surface passivation step is then carried out by contacting the material with a passivating gas. The furnace is then cooled down to room temperature over several hours. The atmosphere is then switched over to air gradually over a period of two hours by switching the gas flow from nitrogen to air from a compressed air supply.
As an example of a fluidized bed reactor method (production scale), 50 g of a particulate porous carbon framework was placed in a fluidized bed reactor fabricated with a 0.95 cm (⅜″) stainless steel gas inlet, a 60 mm outside diameter (O.D.) tubular section with length of 520 mm, and a stainless steel expanded head with an O.D. of 100 mm. The reactor was suspended from a frame and a vertically-oriented tube furnace was positioned such that the hot zone ran from the conical section to ¾ of the length of the cylindrical section (approx. 380 mm long). The minimum fluidization velocity was determined with a cold-flow pressure-drop test with nitrogen as an inert gas, ramping gas flow rate between 1 to 2.5 L/min. Once minimum fluidizing velocity was determined, the inert gas flow rate was held constant at or above the minimum fluidizing velocity. The furnace was ramped to the desired reaction temperature under constant inert gas flow rate. After stabilizing at a target temperature between 435-500° C., the fluidizing gas was switched from pure nitrogen to 1.25 vol% monosilane in nitrogen. The reaction progress was monitored by measuring pressure drop and furnace temperature difference between top and bottom. The gas flow rate was adjusted throughout the run to maintain a pressure drop consistent with continued fluidization and minimum temperature difference between the top and bottom of the bed of less than 40° C. was maintained. After 12 hours, the fluidizing gas was then switched to pure nitrogen whilst maintaining fluidisation, this purge lasted 30 minutes. Optionally, a surface passivation step is then carried out by contacting the material with a passivating gas. Then the furnace was ramped to ambient temperature over several hours. On reaching ambient temperature, the furnace atmosphere was switched to air gradually over a period of hours.
As an example of a reduced pressure fluidized bed reactor method (production scale), 250 g of a particulate porous carbon framework is placed into a fluidized bed reactor fabricated with multiple nozzles designed for horizontal gas injection with a jet velocity of 0.5 - 2 m/s into a 89 mm outside diameter (O.D.) tubular reactor section with length of 1100 mm, and a stainless steel expanded head with an O.D. of 457 mm. The reactor is suspended from a frame and a vertically-oriented tube furnace is positioned such that the hot zone runs from the conical section across the full length of the cylindrical section (approx. 380 mm long). The reactor vessel is vibrated at frequency of 5-140 Hz. The porous carbon particles are fluidized using 10 sL/min (standard litres per minute) of nitrogen as an inert gas, at a pressure of 38 kPa (absolute). The furnace is ramped to a temperature of 450° C. under constant inert gas flow rate. The gas flow is then slowly switched to a mixture of 2 sL/min monosilane (SiH4) and 9 sL/min nitrogen. The rate of silicon deposition is monitored by measuring the hydrogen vol% in the effluent gas over time. Once ca. 200 g silicon is deposited (ca. 45 wt% Si), the gas flow is switched to a mixture of 0.5 sL/min monosilane (SiH4) and 9 sL/min nitrogen until ca. 250 g of silicon is deposited (ca. 49.5 to 51.5 wt% Si). The fluidizing gas is then switched to pure nitrogen whilst maintaining fluidisation for ca. 30 minutes to purge the reactor. Optionally, a surface passivation step is then carried out by contacting the material with a passivating gas. Then the furnace is ramped to ambient temperature over several hours. On reaching ambient temperature, the furnace atmosphere is switched to air gradually over a period of hours.
Porous carbon frameworks C1 to C7 used in the following examples have the characteristics set out in Table 1.
Silicon-carbon composite particles were prepared by placing 1.8 g of a particulate porous framework with the properties listed in Table 1 on a stainless-steel plate at a constant thickness of 1 mm along its length. The plate was then placed inside a stainless-steel tube of outer diameter 60 mm with gas inlet and outlet lines located in the hot zone of a retort furnace. The furnace tube was purged with nitrogen gas for 30 minutes at room temperature, then the sample temperature was increased to between 450 and 475° C. The nitrogen gas flow-rate is adjusted to ensure a gas residence time of at least 90 seconds in the furnace tube and maintained at that rate for 30 minutes. Then, the gas supply is switched from nitrogen to a mixture of monosilane in nitrogen at 1.25 vol. % concentration. Dosing of monosilane is performed over a period of up to 5-hours with a reactor pressure maintained at 101.3 kPa (1 atm). After dosing has finished the gas flow rate is kept constant whilst the silane is purged from the furnace using nitrogen. The furnace is purged for 30 minutes under nitrogen before being cooled down to room temperature over several hours. The atmosphere is then switched over to air gradually over a period of two hours by switching the gas flow from nitrogen to air from a compressed air supply.
A series of samples of composite particles with varying amounts of deposited silicon (varying between 20 and 60 wt%) were made using the method of Example 1 using each of the carbons in Table 1. The Surface Silicon was calculated from the TGA curve for each sample. Table 2 provides the mean, maximum and minimum values of the Surface Silicon for the group of samples made with each carbon. It can be seen that very small or inconsistent amounts of Surface Silicon could be achieved using carbons C1, C2 and C7 whilst good levels of Surface Silicon could be consistently achieved across all samples with carbons C3, C5 and C6.
The data from these experiments are shown in
Silicon-carbon composite particles were prepared in a vertical bubble-fluidized bed reactor comprising an 83 mm internal diameter stainless steel cylindrical vessel operating at atmospheric pressure. A 250 g quantity of a powder of carbon framework particles with the properties listed in Table 1 is placed in the reactor. An inert gas (nitrogen) at a low flow rate is injected into the reactor to remove any oxygen. The reactor is then heated to a reaction temperature between 430 and 500° C. and 4% v/v monosilane gas diluted in nitrogen is supplied to the bottom of the reactor at a flow rate sufficient to fluidize the carbon framework particles, for a length of time sufficient to deposit the target mass of silicon. The reactor is purged for 30 minutes under nitrogen before being cooled down to room temperature over several hours. The atmosphere is then switched over to air gradually over a period of two hours by switching the gas flow from nitrogen to air from a compressed air supply.
Silicon-carbon composite particles were prepared in a vertical bubble-fluidized bed reactor comprising a 83 mm internal diameter stainless steel cylindrical vessel. A 250 g quantity of a powder of carbon framework particles with the properties listed in Table 1 is placed in the reactor. The porous carbon particles are fluidized using 10 sL/min (standard litres per minute) of nitrogen as an inert gas, at a pressure of 38 kPa (absolute). The furnace is ramped to a temperature of 450° C. under constant inert gas flow rate. The gas flow is then slowly switched to a mixture of 2 sL/min monosilane (SiH4) and 9 sL/min nitrogen. The rate of silicon deposition is monitored by measuring the hydrogen vol% in the effluent gas over time. Once ca. 200 g silicon is deposited (ca. 45 wt% Si), the gas flow is switched to a mixture of 0.5 sL/min monosilane (SiH4) and 9 sL/min nitrogen until ca. 250 g of silicon is deposited (ca. 49.5 to 51.5 wt% Si). The fluidizing gas is then switched to 10 sL/min of pure nitrogen whilst maintaining fluidisation for ca. 30 minutes to purge the reactor. The fluidizing gas is then switched to a mixture of 2 sL/min of ethylene (C2H4) and 9 sL/min nitrogen to passivate the silicon surface. The fluidizing gas is then switched to 4 sL/min of pure nitrogen. Then the furnace is cooled to ambient temperature over several hours. On reaching ambient temperature, the furnace atmosphere is switched to air gradually over a period of hours.
A mass of composite particles made using the method of Example 3 were placed into a stainless-steel tube loaded into a rotary furnace tube and sealed. The reactor space was purged with nitrogen at 0.2 L/min for 30 min. The furnace temperature was ramped up to 675° C. under nitrogen flow. A measured amount of styrene was placed in a Dreschel bottle and heated in a water bath, up to 75° C. After 10 minutes of furnace temperature stabilisation, styrene was allowed to flow into the reactor tube for 90 minutes by bubbling nitrogen of 2 L/min into the Dreschel bottle. The reactor is then purged with nitrogen and cooled down to ambient temperature under nitrogen, resulting in a carbon coated material.
The procedure used to calculate the surface silicon and coarse bulk silicon for the composite materials of the examples was as follows. 10 mg (±2 mg) of the sample under test was loaded into a 70 µL crucible. The sample was loaded into a Mettler Toledo TGA/DSC 3+ instrument with an Ar purge gas, N2 padding gas and air reaction gas at 100 mL/min. The TGA furnace chamber was ramped from 25 to 1400° C. at a rate of 10° C./min. Data was collected at 1 s intervals. With reference to
Negative electrode coatings (anodes) were prepared using the Si-C composite materials of Table 3 and tested in full coin cells. To make the electrodes, a dispersion of carbon black in CMC binder was mixed in a Thinky™ mixer. The Si-C composite material was added to the mixture and mixed for 30 min in the Thinky™ mixer. SBR binder was then added to give a CMC: SBR ratio of 1:1, yielding a slurry with a weight ratio of Si-C composite material: CMC/SBR: carbon black of 70%:16%:14%. The slurry was further mixed for 30 min in the Thinky™ mixer, then was coated onto a 10 µm thick copper substrate (current collector) and dried at 50° C. for 10 minutes, followed by further drying at 110° C. for 12 hours to thereby form a negative electrode with a coating density of 0.7 ± 0.5 g/cm3.
Full coin cells were made using circular negative electrodes of 0.8 cm radius cut from the negative electrodes with a porous polyethylene separator and a nickel manganese cobalt (NMC532) positive electrode. The positive and negative electrodes were designed to form a balanced pair, such that the capacity ratio of the positive to negative electrodes was 0.9. An electrolyte comprising 1 M LiPF6 in a solution of fluoroethylene carbonate, ethylene carbonate and ethyl methyl carbonate containing 3 wt% vinylene carbonate was then added to the cell before sealing.
The coin cells were cycled as follows: A constant current was applied at a rate of C/25, to lithiate the anode, with a cut off voltage of 4.3 V. When the cut off was reached, a constant voltage of 4.3 V is applied until a cut off current of C/100 is reached. The cell was then rested for 10 minutes in the lithiated state. The anode is then delithiated at a constant current of C/25 with a cut off voltage of 2.75 V. The cell was then rested for 10 minutes. After this initial cycle, a constant current of C/2 was applied to lithiate the anode with a 4.3 V cut off voltage, followed by a 4.3 V constant voltage with a cut off current of C/40 with rest time of 5 minutes. The anode was then delithiated at a constant current of C/2 with a 2.75 V cut off. This was then repeated for the desired number of cycles. The capacity retention at 100 cycles (CR100) and 500 cycles (CR500) was calculated and is given in Table 4 along with the 1st lithiation capacity, the 1st delithiation capacity and the first cycle loss (FCL).
The charge (lithiation) and discharge (delithiation) capacities for each cycle are calculated per unit mass of the silicon-carbon composite material and the capacity retention value is calculated for each discharge capacity as a percentage of the discharge capacity on the second cycle. The first cycle loss (FCL) is (1 - (1st delithiation capacity/1st lithiation capacity)) x 100%. The values in Table 4 are averaged over 3 coin cells for each material.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2012061.4 | Aug 2020 | GB | national |
| 2104460.7 | Mar 2021 | GB | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/GB2021/052005 | 8/3/2021 | WO |
