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Process parameter

At the process conditions of SFE, the solvent capacity in general increases with pressure at constant temperature. Therefore, the amount of extract after a certain time of extraction will increase with pressure. Note that increasing pressure increases solvent power. For mixtures of extract compounds this will result in different extracted compositions at different pressures. [Pg.92]

With increasing density, the extraction rate increases at constant temperature. Density is responsible for the capacity and solvent power of a solvent, as the solubility of a compound rises wiA increasing density. In the extraction process, mass transfer is also of importance. Therefore, the extraction results will be different for the sanie density at different temperatures. [Pg.93]

The solvent ratio is the most important parameter for technical applications of SFE, once approximate values of pressure and temperature have been selected. With increasing solvent ratio the extraction rate can be enhanced more than by changing process parameters within relatively narrow limits. The influence of the solvent ratio must be discussed while also considering the economic consequences [1] which are beyond the scope of this chapter. [Pg.93]

Mass transfer in extraction from solid substrates in most cases depends heavily on the transport rate in the solid phase. The length of the transport path determines mass transport in the solid phase. In general the extraction rate increases with decreasing particle size. However, mass transfer into the fluid phase has to be achieved. If the smaller particles hinder the flow of the fluid in the fixed bed, then the mass transfer rate and the amount of extract decrease with smaller particles. [Pg.93]

Key process parameters and feedstock requirements for each technology include the following  [Pg.337]

PRESSURE - Most SMR plants run at reformer outlet pressures between 150 and 400 psig. The maximum pressure is about 550 psig, due to metallurgical considerations in the SMR outlet piping. The same applies to SMR/O2R plants. [Pg.337]

This limits the final product gas pressure to about 500 psig. Above this, product gas compression is required. [Pg.337]

ATR and POX plants can run at much higher pressures. For example, some plants require synthesis gas at about 800 psig this can be supplied directly from an ATR or POX without synthesis gas compression. TEMPERATURE - SMR plants typically run at reformer outlet temperatures of 1550 to 1700°F. [Pg.337]

POX plants typically run at about 2500°F. This high temperature is needed to maintain low residual methane without a catalyst. STEAM/CARBON - Steam is typically required to prevent carbon formation on the reformer catalyst. The steam requirement is generally expressed as the steam/hydrocarbon-carbon ratio (steam/hcc). This is the ratio of the moles of steam to moles of hydrocarbon-carbon in the feed (the carbon in any CO2 recycle is not included in computation of the ratio). [Pg.337]

Typical operating parameters suggested in the EPA standard method are listed in Table 3.7. [Pg.159]

As mentioned before, solubility and mass transfer increase at elevated temperatures. Table 3.8 shows that both recovery and precision improved when the temperature was increased during the extraction of total petroleum [Pg.159]

The general criteria for the solvent selection are high solubility of the analytes and low solubility of the sample matrix. Solvents used in conventional [Pg.160]

Reproduced from Ref. 46, with permission from the American Chemical Society. [Pg.160]

Organochlorine pesti- Acetone-hexane (1 1 v/v) or acetone-methylene chloride [Pg.161]

There are many factors that govern the mechanical and electrical design and performance of a supercritical carbon dioxide (SCF) system. Some of the process parameters that may influence system design are shown in Table 1. [Pg.246]

These considerations determine the design features and operational requirements of the supercritical carbon dioxide system and hence its costs. Most suppliers have laboratory facilities in which a customer s parts can be tested to determine the appropriate cleaning parameters. [Pg.246]

Level of cleanliness required Temperature, pressure, separator efficiency, cycle time [Pg.247]

Type and amount of organic contaminant Temperature, pressure, co-solvents [Pg.247]

composition and amount of particulate Flow rate, agitation, filtration [Pg.247]

Level of cleanliness required Type and amount of organic contaminant Type, size, composition and amount of particulate contaminant Co-solvent requirements Type of parts to be cleaned (e.g., size, complexity, porosity, loading density, pressure sensitivity) Production capacity Breadth of application Temperature, pressure, separator efficiency, cycle time Temperature, pressure, co-solvents Flow rate, agitation, filtration Type, quantity, emission control and recycle considerations Dimensions, fixturing and flow pattern within cleaning vessel process control strategy Parts per cycle and cycles per work period Number of different processes that must be performed by the system [Pg.247]

System Type. The three basic types of SCF cleaning systems are the direct system, in which supercritical carbon dioxide (SCCO2) is the only cleaning solvent, the single-cycle system, in which the SCCO2 is mixed with a cosolvent and the dual-cycle system in which the parts are exposed separately to cosolvent and supercritical carbon dioxide. [Pg.248]

Direct Removal Using SCCOy This is the least expensive option. This system uses liquid carbon dioxide or supercritical carbon dioxide to remove contaminants directly from the parts or to remove residual solvent from a separate, non-carbon-dioxide cleaning process. [Pg.248]

An efficient operation of an AOP depends on both the nature of waste and the type of AOP used. The optimum conditions are determined individually through treatability studies and pilot testing. The process parameters can be broadly divided under the following categories (a) characteristics of wastewater and (b) operating conditions. [Pg.469]

As discussed earlier, organic compounds with double bonds, especially with chlorine, react quickly with hydroxyl radical. On the other hand, saturated organic compounds such as 1,1-dichloroethane and chloroform, are better removed by UV photolysis. Depending on the type of organic compound, initial contaminant concentration will affect the performance of the process. For high contaminant level, multiple AOPs can be used. For example, for a COD 5000 mg/L, sequential treatment using Fenton s reagent followed by UV oxidation may be chosen. [Pg.469]

The pH of water is an important factor for AOP application in the water phase as the hydroxyl radical concentration is a function of pH. pH controls the equilibrium of carbonate, bicarbonate, and carbonic acid present in water carbonate and bicarbonate both scavenge hydroxyl radicals with rate constants of 3.9 x 10 M s and 8.5 x 10 M s , respectively. Thus, acidic pH is better for water with high carbonate and bicarbonate alkahnity (greater than 400 mg/L as CaCOg). However, the effect of pH is system-specific for example, generally UV/H2O2 is more effective at low pH, while UV/O3 is more effective at slightly basic pH. [Pg.470]

The aqueous stream being treated must provide for good transmission of UV light (high turbidity causes interference). This factor can be more critical for UV/HgOg than UV/O3. Sonodegradation rate also is reported to be affected by turbidity. However, turbidity does not affect direct chemical oxidation of the contaminant by HgOg or ozone. Water with suspended solids above 300 mg/L needs pretreatment to remove the sohds for UV oxidation. [Pg.470]

The aqueous stream to be treated by UV/oxidation should be relatively free of heavy metal ions (less than 10 mg/L) and insoluble oil or grease to minimize the potential for fouling of the quartz sleeves. In some waters, a small change in pH causes soluble inorganic chemicals such as calcium, iron, and manganese to precipitate. Heavy metals oxidized by hydroxyl radical cause additional concern. Eor example, Cr + is more toxic than Cr3+. [Pg.470]

The concentration and qualities of the reactants (i.e., silver nitrate, ammonia, sodium azide), as given, are not critical and could probably be varied by a factor of two. The concentration of the ammonia (presently 3 N) would have to be adjusted to maintain the solubility of the silver azide. For instance, a 200 g/liter concentration of silver azide in a 5 N ammonium hydroxide could easily be achieved as a starting mother liquor. In the present process the 120 g/liter concentration of silver azide represents a 10-fold increase in productivity over the Taylor process [3]. [Pg.51]

Vigorous agitation during evaporation is very eritieal. Preliminary tests showed that a reduetion of bulk density and an inerease in large flat erystals oeeurs unless the agitation produees turbulenee, partieularly top to bottom turnover. [Pg.52]

The seleeted time-temperature program evolved direetly from the avoidanee [Pg.52]

The quantity of acetic acid added for seeding was suitable for achieving uniform bulk density and desirable granulation range of the product. Silver azide is quite resistant to acetic acid. Its addition results in profuse nucleation. [Pg.53]

The second addition of acetic acid serves the purpose of neutralizing the last traces of ammonia in the mother liquor and reduces losses of valuable silver in the mother liquor. [Pg.53]

The amount of incorporated particles is the parameter characterizing a metal matrix composite. As discussed in the previous section it largely determines the composite properties. In order to obtain a composite exhibiting certain properties, the effect of process parameters on the particle composite content has therefore to be known. Apart from the practical significance knowledge of these effects is also a prerequisite for the understanding of the mechanism underlying particle codeposition. [Pg.483]

Through the years it has been found that numerous process parameters directly or indirectly affect the particle composite content. These parameters can be divided into three main categories  [Pg.483]

A straightforward effect of a single parameter on the particle composite content can not always be given, because the influence of several parameters is interrelated. The fact that some parameters have been investigated extensively, whereas others were hardly examined even [Pg.483]

The mechanism of particle incorporation is treated extensively in the next section, but a generalized mechanism is given here to better comprehend the effects of the process parameters. Particle incorporation in a metal matrix is a two step process, involving particle mass transfer from the bulk of the suspension to the electrode surface followed by a particle-electrode interaction leading to particle incorporation. It can easily be understood that electrolyte agitation, viscosity, particle bath concentration, particle density etc affect particle mass transfer. The particle-electrode interaction depends on the particle surface properties, which are determined by the particle type and bath composition, pH etc., and the metal surface composition, which depends on the electroplating process parameters, like pH, current density and bath constituents. The particle-electrode interaction is in competition with particle removal from the electrode surface by the suspension hydrodynamics. [Pg.484]

All these treatments exert their effect by controlled crystal growth, e.g. larger, fewer crystals adsorb less liquid fat and there is less formation of mixed (liquid-solid) crystals due to reduced supercooling. [Pg.137]

Fractionation. The melting and spreading characteristics of butter can be altered by fractional crystallization, i.e. controlled crystallization of molten fat or crystallization from a solution of fat in an organic solvent (e.g. ethanol or acetone). Cleaner, sharper fractionation is obtained in the latter but solvents may not be acceptable for use with foods. The crystals formed may [Pg.137]

Blending. Blends of vegetable oils and milk fat offer an obvious solution to the problem of butter hardness - any desired hardness values can be obtained. Such products were introduced in the 1960 s and are now used widely in many countries. These products may be produced by blending an [Pg.138]

In addition to modifying the rheological properties of butter, blends of milk fat and vegetable oils can be produced at a reduced cost (depending on the price paid for milk fat) and have an increased content of polyunsaturated fatty acids, which probably has a nutritional advantage. Oils rich in CO-3 fatty acids, which are considered to have desirable nutritional properties, may be included in the blend, although these oils may be susceptible to oxidative rancidity. [Pg.139]

Low-fat spreads. Spreads containing 40% fat (milk fat or blends of milk fat and vegetable oils), c. 3-5% protein and selected emulsifiers are now commonly available in many countries. These products have good spreada-bility and reduced caloric density (see Keogh, 1995). [Pg.139]

This review of chemorheological techniques highlights the numerous possibilities for monitoring chemoviscosity and gel-point measurements. Determination of the appropriate techniques must be based on the following considerations  [Pg.344]

The selection of the optimum chemorheological techniques can then be used to influence the choice of rheometer for chemorheological measurements. Final selection of the rheometer design must be determined by the considerations given in the previous section, as well as the following  [Pg.344]

One of the key transitions that also needs to be characterized is gelation. The physical nature and models of gelation have been described in Chapter 2, so here we wish to examine the methods used to determine gelation. The determination of the gel point of thermosets may be monitored by the following methods  [Pg.345]

For the further reduction of the reaction volume we tested even higher substrate concentrations and higher concentrated titrating solutions. As to the former, it turned out that the enzyme worked smoothly even at 20 to 30% (w/v) substrate concentration and, in addition, at substrate to buffer ratio of 1 1 (w/v) the enzyme still showed a useful activity. In all cases the product was obtained with excellent chemical and enantiomeric purity (both 99%). [Pg.391]

As to the concentration of the titrating solution a high NaOH concentration affected the enzyme activity more seriously than a high substrate concentration. Thus, in order to have a high space-time yield it is better to work with a high substrate concentration and titrate with a moderately concentrated sodium hydroxide solution than vice versa. However, at pH 9 the enzyme still worked without problems at 33% substrate concentration using 3 M or 4 M sodium hydroxide solution (and even 9 M NaOH worked, however, with a considerably reduced enzyme activity). [Pg.391]

39 °C) it was necessary to keep the temperature at a minimum of 37 °C, thus limiting the useful temperature range to 38-43 °C. [Pg.392]

Because at very high substrate and sodium hydroxide concentrations work-up became more tedious due to persistent emulsions, an initial substrate concentration of 20-30% together with 3 M NaOH seemed to be optimal. On the pilot-scale, however, we had to choose a certain filling level of the reaction vessel (a 1000 L fermenter) in order to achieve optimal stirring and, therefore, pilot runs were sometimes conducted at sub-optimal substrate and NaOH concentrations. For the same reasons we defined a broad acceptable range of concentrations. [Pg.392]

Based on the above results the following optimal conditions were specified for the enzyme reaction 25-50 g of 2 emulsified in 100 mL of buffer pH 8.5 at 39-43 °C using a 2-4 M NaOH solution for pH control. [Pg.392]

Parameter Unit Quartz Stuben Sandstone Jurassic Limestone Triassic Limestone [Pg.126]

Result of a linearisation of the associated Freundlich isotherm with respect to Tantamount to rate of easy accessible sorption sites (approximated via ratio of inner and outer grain surface). [Pg.126]

If the material is porous, the liquid will penetrate into the pores when wetting occurs (9 90°). This can be described by the Laplace equation  [Pg.367]

If 9 90° then cos 9 0 and Ap 0, and only if a finite pressure is applied (according to the Laplace equation) the liquid will penetrate into the membrane. As can be seen from eq. VI -110, the wettability depends on three factors  [Pg.367]

When a liquid is brought into contact with a (smooth) polymeric surface, various contact angles between the liquid and the polymer are observed depending on the affinity between the liquid and the polymer. Three different cases can be distinguished as shown in figure VI - 49. If the contact angle is greater than 90 , the liquid does not wet the [Pg.368]

The applications are determined by the wettabilin of the membrane, which implies that mainly aqueous solutions containing inorganic solutes can be treated. The surface tension of these solutions differs little fi-om that of water. The applications can be classified as to whether i) permeate is the desired product or ii) retentate is the desired product. [Pg.370]

In most applications the prameateis the product of interest. A high quality permeate can be obtained with membrane distillation, as for example [79] [Pg.370]

It must be emphasized that corrosion is likely to occur only in the water phase. Vaporized water in streams at temperatures above the dew point are considered non-corrosive. [Pg.97]


To realize a process integrated quality control the conception shown in fig. 2 was followed. The casting process which is influenced by process parameters like thermal economy, alloy composition or black wash will be pursued with particulary to the problematic nature adjusted sensoring systems. On basic factors orientated sensoring systems like microfocus radioscopy, and tomography will be employed and correlated with sensoring systems which can be applicated under industrial conditions. [Pg.11]

Those, on industrial applications orientated systems, are acoustic emission and the temperature analysis of the casting. Realizing this conception (fig. 2) will enable to develop a process parameter control and consequently to stabilize the casting process. [Pg.11]

If improvements should be achieved by an automation of the inspection process this requires a control of the process parameters of the whole equipment by an integrated "intelligent" system and not by displays still being controlled by the human inspector. This integrated control-system ensures that the inspection conditions are at the highest reproduction level. [Pg.628]

To operate the MPI or LPI equipment at stable and reprodncable inspection conditions modern units are equipped with a monitoring and control system called "Quality Assurance Package" (termed QAP). The QAP System is ba.sed on an industrial PC with a bus system and field sensors. It ensures that process parameters important for the reproducability of the MPI or LPI are controlled an held between defined limits by a central computer system. It can be adapted to any old system, as well as integrated into new systems. [Pg.628]

For calculation of the volumetric flow rate only the cross section area of the pipe is to be known. In order to give flow under standard conditions the temperature and pressure must be measured, and for conversion to mass flow the composition or density of the gas must be determined. These process parameters are often monitored by calibrated instrumentation. [Pg.1054]

Mechanical Properties. Polyester fibers are formed by melt spinning generally followed by hot drawing and heat setting to the final fiber form. The molecular orientation and crystalline fine stmcture developed depend on key process parameters in all fiber formation steps and are critical to the end use appHcation of the fibers. [Pg.326]

The effect of mechanical treatment on floe behavior is illustrated in Figure 5. In one work (40), identical slurries were treated with varying doses of the same polymer. At each dosage, it can be assumed that the same type of floe formed at the same rate. However, the dosage response was completely different depending on which parameter of the flocculated slurry was measured. Thus the term optimal flocculation caimot be appHed to any flocculant—substrate combination if the soHd—Hquid separation process or process parameter is not specified. [Pg.35]

Combustion. Coal combustion, not being in the strictest sense a process for the generation of gaseous synfuels, is nevertheless an important use of coal as a source of gaseous fuels. Coal combustion, an old art and probably the oldest known use of this fossil fuel, is an accumulation of complex chemical and physical phenomena. The complexity of coal itself and the variable process parameters all contribute to the overall process (8,10,47—50) (see also COLffiUSTION SCIENCE AND technology). [Pg.72]

Item Study node Process parameters Deviations (Guide words) Possible causes Possible consequences Action required Assigned to i i... [Pg.472]

Fig. 12. Critical process parameters as a function of gas enthalpy where A is yield, B is concentration, and C is the specific energy requirement (SER). Fig. 12. Critical process parameters as a function of gas enthalpy where A is yield, B is concentration, and C is the specific energy requirement (SER).
The performance of SCWO for waste treatment has been demonstrated (15,16). In these studies, a broad number of refractory materials such as chlorinated solvents, polychlorinated biphenyls (PCBs), and pesticides were studied as a function of process parameters (17). The success of these early studies led to pilot studies which showed that chlorinated hydrocarbons, including 1,1,1-trichloroethane /7/-T5-6y,(9-chlorotoluene [95-49-8] and hexachlorocyclohexane, could be destroyed to greater than 99.99997, 99.998, and 99.9993%, respectively. In addition, no traces of organic material could be detected in the gaseous phase, which consisted of carbon dioxide and unreacted oxygen. The pilot unit had a capacity of 3 L/min of Hquid effluent and was operated for a maximum of 24 h. [Pg.499]

The process of growing a pure crystal is sensitive to a host of process parameters that impact the iacorporation of impurities ia the crystal, the quality of the crystal stmcture, and the mechanical properties of the crystal rod. For example, the crystal-pulling mechanism controls the pull rate of the crystallisa tion, which affects the iacorporation of impurities ia the crystal, and the crystal rotation, which affects the crystal stmcture. [Pg.346]

Theoretical studies of diffusion aim to predict the distribution profile of an exposed substrate given the known process parameters of concentration, temperature, crystal orientation, dopant properties, etc. On an atomic level, diffusion of a dopant in a siUcon crystal is caused by the movement of the introduced element that is allowed by the available vacancies or defects in the crystal. Both host atoms and impurity atoms can enter vacancies. Movement of a host atom from one lattice site to a vacancy is called self-diffusion. The same movement by a dopant is called impurity diffusion. If an atom does not form a covalent bond with siUcon, the atom can occupy in interstitial site and then subsequently displace a lattice-site atom. This latter movement is beheved to be the dominant mechanism for diffusion of the common dopant atoms, P, B, As, and Sb (26). [Pg.349]

Ionomer resins are produced in multiple grades to meet market needs, and prospective customers are provided with information on key processing parameters such as melt-flow index. Nominal values for many other properties are Hsted in product brochures. The ASTM test methods developed for general-purpose thermoplastic resins are appHcable to ionomers. No special methods have been introduced specifically for the ionomers. [Pg.408]

Slurry Viscosity. Viscosities of magnesium hydroxide slurries are determined by the Brookfield Viscometer in which viscosity is measured using various combinations of spindles and spindle speeds, or other common methods of viscometry. Viscosity decreases with increasing rate of shear. Fluids, such as magnesium hydroxide slurry, that exhibit this type of rheological behavior are termed pseudoplastic. The viscosities obtained can be correlated with product or process parameters. Details of viscosity deterrnination for slurries are well covered in the Hterature (85,86). [Pg.350]

The second step is to disperse the core material being encapsulated in the solution of shell material. The core material usually is a hydrophobic or water-knmiscible oil, although soHd powders have been encapsulated. A suitable emulsifier is used to aid formation of the dispersion or emulsion. In the case of oil core materials, the oil phase is typically reduced to a drop size of 1—3 p.m. Once a suitable dispersion or emulsion has been prepared, it is sprayed into a heated chamber. The small droplets produced have a high surface area and are rapidly converted by desolvation in the chamber to a fine powder. Residence time in the spray-drying chamber is 30 s or less. Inlet and outlet air temperatures are important process parameters as is relative humidity of the inlet air stream. [Pg.322]

Process parameters can be varied to change the MDA isomer distribution and oligomeric content of PMDA products. Generally, aniline to formaldehyde molar ratios of 2 to 5 are used. To increase the MDA content, higher ratios of aniline to formaldehyde are employed. Increasing the acid to aniline ratio also increases the 4,4 -MDA content of the diamine fraction. Historically, the polyurethane industry consumes as much of the 4,4 -MDI isomer as possible. Recently, however, there has been an increasing demand for higher 2,4 -MDI and 2,4 -PMDI products to be used as replacements for... [Pg.249]

It is becoming more and more desirable for the analytical chemist to move away from the laboratory and iato the field via ia-field instmments and remote, poiat of use, measurements. As a result, process analytical chemistry has undergone an offensive thmst ia regard to problem solviag capabihty (77—79). In situ analysis enables the study of key process parameters for the purpose of definition and subsequent optimization. On-line analysis capabihty has already been extended to gc, Ic, ms, and ftir techniques as well as to icp-emission spectroscopy, flow iajection analysis, and near iafrared spectrophotometry (80). [Pg.397]

Statistical Process Control. A properly miming production process is characterized by the random variation of the process parameters for a series of lots or measurements. The SPG approach is a statistical technique used to monitor variation in a process. If the variation is not random, action is taken to locate and eliminate the cause of the lack of randomness, returning the process or measurement to a state of statistical control, ie, of exhibiting only random variation. [Pg.366]

Many more suppHers and information about their product line can be obtained from compilations such as the Modem Plastics Pmyclopedia (1) and the Thomas Register of Mmerican Manufacturers (2). The choice of a release agent depends on the process conditions involved and the nature of the contacting substrates (3). Apart from the obvious ease of release, other important requirements are minimal buildup of residues on mold substrate, minimal effect on the molded article, adequate film-forming abiHty, compatibiHty with secondary operations and other processing parameters, health and safety requirements, and cost. [Pg.99]

Measurable Process Parameters. The RO process is relatively simple ia design. It consists of a feed water source, feed pretreatment, high pressure pump, RO membrane modules, and ia some cases, post-treatment steps. A schematic of the RO process is shown ia Figure 2a. [Pg.145]

Effects of Rate Conditions. It is essential for commercial a-quartz crystals to have usable perfection growth at a high rate and at pressure and temperature conditions that allow economical equipment design. The dependence of rate on the process parameters has been studied (8,14) and may be summarized as follows. Growth rate depends on crystallographic direction the (0001) is one of the fastest directions. Because AS is approximately linear with AT, the growth rate is linear with AT. Growth rate has an Arrhenius equation dependence on the temperature in the crystallization zone ... [Pg.520]

The thermal decomposition of silanes in the presence of hydrogen into siUcon for production of ultrapure, semiconductor-grade siUcon has become an important art, known as the Siemens process (13). A variety of process parameters, which usually include the introduction of hydrogen, have been studied. Silane can be used to deposit siUcon at temperatures below 1000°C (14). Dichlorosilane deposits siUcon at 1000—1150°C (15,16). Ttichlorosilane has been reported as a source for siUcon deposition at >1150° C (17). Tribromosilane is ordinarily a source for siUcon deposition at 600—800°C (18). Thin-film deposition of siUcon metal from silane and disilane takes place at temperatures as low as 640°C, but results in amorphous hydrogenated siUcon (19). [Pg.22]

Monitoring by Electromechanical Instrumentation. According to basic engineering principles, no process can be conducted safely and effectively unless instantaneous information is available about its conditions. AH sterilizers are equipped with gauges, sensors (qv), and timers for the measurement of the various critical process parameters. More and more sterilizers are equipped with computerized control to eliminate the possibiUty of human error. However, electromechanical instmmentation is subject to random breakdowns or drifts from caUbrated settings and requires regular preventive maintenance procedures. [Pg.406]


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Process parameters liquid products composition

Process parameters liquid products yield

Process parameters methane conversion

Process parameters methanol formation

Process parameters methanol formation selectivity

Process parameters methanol selectivity

Process parameters methanol yield

Process parameters minimal temperature dependence

Process parameters oxygen concentration

Process parameters particle size

Process parameters pressure dependence

Process parameters quartz reactor

Process parameters reaction product kinetics

Process parameters reaction time

Process parameters reactor surface temperature

Process parameters residence time

Process parameters sample dimensions

Process parameters screen printing

Process parameters stainless steel reactor

Process parameters static reactor

Process parameters temperature dependence

Process parameters temperature profile

Process parameters thermodynamics

Process parameters time history, temperature

Process parameters total yield

Process parameters, advanced electric

Process parameters, relation

Process safety analysis parameters

Process simulation—steady state equipment parameters

Process system design parameters

Process-control parameters from time-temperature superposition

Processes parameters for

Processing Parameters and the Rate of Resorption

Processing Parameters for Commonly Used Binders

Processing of the simulation output parameters

Processing parameter, viii

Processing parameters

Processing parameters

Processing parameters general scheme

Processing, thermoplastics molding parameters

Product design process parameters

Quantitative Control of Chemical Vapour Deposition Process Parameters

Resist processing controllable parameters

Short-contact-time process parameters

Slow pyrolysis process parameters

Some important process parameters

Soot formation processes parameters

Spectral parameter fitting processes

Tables with recommended processing parameters

Technological parameters of formation process

The influence of processing parameters on injection-moulded PET

Treatment process parameters

Two-Dimensional NMR Data-Processing Parameters

Ultrasonic welding processing parameters

Use of Process-intensifying Parameters

Ventilation Parameters That Influence the Building Construction and Process Design

Verification of Model Parameters Prior to Process Simulation

Volume recovery process parameter

Volume recovery process rate parameter

Weber number process parameters

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