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heuristics in chemical engineering onedited for on-line use by g j suppes february 2002 reproduced with permission from butterworthbutterworth-heinemann material from chemical process equipment selection and design by stanley m walas butterworth thpublished by butterworth-heinemann boston 1990 heuristics in chemical engineering although experienced engineers know where to find information and how to make accurate computations they also keep a minimum body of information in mind on the ready made up largely of shortcuts and heuristics the present compilation may fit into such a minimum body of information as a boost to the memory or extension in some instances into less often encountered areas an engineering rule of thumb is an outright statement regarding suitable sizes or performance of equipment that obviates all need for extended calculations because any brief statements are subject to varying degrees of qualification they are most safely applied by engineers who are substantially familiar with the topics nevertheless such rules should be of value for approximate design and cost estimation and should provide even the inexperienced engineer with perspective and a foundation whereby the reasonableness of detailed and computer-aided results can be appraised quickly particularly on short notice such as in conference much more can be stated in adequate summary fashion about some topics than about others which accounts in part for the spottiness of the present coverage accordingly every engineer undoubtedly will supplement or modify this material in his/her own way.

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heuristics by topic · · · · · · · · · · · · · · · · · · · · · · · · · · · compressors and vacuum pumps conveyors for particulate solids cooling towers crystallization from solution disintegration distillation and gas absorption a distillation and gas absorption b distillation and gas absorption c drivers and power reocvery equipment drying of solids evaporators extraction liquid-liquid filtration fluidization of particles with gases heat exchangers insulation mixing and agitation particle size enlargement piping pumps reactors refrigeration size separation of particles utilities common specifications vessels drums vessels pressure vessels storage tanks

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-compressors and vacuum pumps1 fans are used to raise the pressure about 3 12 in water blowers raise to less than 40 psig and compressors to higher pressures although the blower range commonly is included in the compressor range 2 vacuum pumps reciprocating piston type decrease the pressure to 1 torr rotary piston down to 0.001 torr two-lobe rotary down to 0.0001 torr steam jet ejectors one stage down to 100 torr three stage down to 1 torr five stage down to 0.05 torr 3 a three-stage ejector needs 100 lb steam/lb air to maintain a pressure of 1 torr 4 in-leakage of air to evacuated equipment depends on the absolute pressure torr and the volume of the equipment v cuft according to w kv2/3 lb/hr with k 0.2 when p is more than 90 torr 0.08 between 3 and 20 torr and 0.025 at less than 1 torr 5 theoretical adiabatic horsepower thp scfmt1/8130a p2/p1a-1 where tl is inlet temperature in °f+460 and a k -1 k k cp/cv 6 outlet temperature t2 t1p2/p1a 7 to compress air from 100 f k 1.4 compression ratio 3 theoretical power required 62 hp/million cuft/day outlet temperature 306°f 8 exit temperature should not exceed 350-400°f for diatomic gases cp/cv 1.4 this corresponds to a compression ratio of about 4 9 compression ratio should be about the same in each stage of a multistage unit ratio pn/p11/n with n stages 10 efficiencies of reciprocating compressors 65 at compression ratio of 1.5 75 at 2.0 and 80-85 at 3-6 11 efficiencies of large centrifugal compressors 6000-100,000 acfm at suction are 76-78 12 rotary compressors have efficiencies of 70 except liquid liner type which have 50 -conveyors for particulate solids1 screw conveyors are suited to transport of even sticky and abrasive solids up inclines of 20° or so they are limited to distances of 150 ft or so because of shaft torque strength a 12 in dia conveyor can handle 1000-3000 cuft/hr at speeds ranging from 40 to 60 rpm 2 belt conveyors are for high capacity and long distances a mile or more but only several hundred feet in a plant up inclines of 30° maximum a 24 in wide belt can carry 3000 cuft/hr at a speed of 100 ft/min but speeds up to 600 ft/min are suited to some materials power consumption is relatively low.

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3 bucket elevators are suited to vertical transport of sticky and abrasive materials with buckets 20 x 20 in capacity can reach 1000 cuft/hr at a speed of 100 ft/min but speeds to 300 ft/min are used 4 drag-type conveyors redler are suited to short distances in any direction and are completely enclosed units range in size from 3 in square to 19 in square and may travel from 30 ft/min fly ash to 250 ft/min grains power requirements are high 5 pneumatic conveyors are for high capacity short distance 400 ft transport simultaneously from several sources to several destinations either vacuum or low pressure 6-12 psig is employed with a range of air velocities from 35 to 120 ft/sec depending on the material and pressure air requirements from 1 to 7 cuft/cuft of solid transferred -cooling towers1 water in contact with air under adiabatic conditions eventually cools to the wet bulb temperature 2 in commercial units 90 of saturation of the air is feasible 3 relative cooling tower size is sensitive to the difference between the exit and wet bulb temperatures 5 15 25 t f relative volume 2.4 1.0 0.55 4 tower fill is of a highly open structure so as to minimize pressure drop which is in standard practice a maximum of 2 in of water 5 water circulation rate is 1-4 gpm/sqft and air rates are 1300-1800 lb hr sqft or 300-400 ft/min 6 chimney-assisted natural draft towers are of hyperboloidal shapes because they have greater strength for a given thickness a tower 250 ft high has concrete walls 5-6 in thick the enlarged cross section at the top aids in dispersion of exit humid air into the atmosphere 7 countercurrent induced draft towers are the most common in process industries they are able to cool water within 2 f of the wet bulb 8 evaporation losses are 1 of the circulation for every 100 f of cooling range windage or drift losses of mechanical draft towers are 0.1-0.3 blowdown of 2.5-3.0 of the circulation is necessary to prevent excessive salt buildup -crystallization from solution1 complete recovery of dissolved solids is obtainable by evaporation but only to the eutectic composition by chilling 2 recovery by melt crystallization also is limited by the eutectic composition.

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3 growth rates and ultimate sizes of crystals are controlled by limiting the extent of supersaturation at any time 4 the ratio s c csat of prevailing concentration to saturation concentration is kept near the range of 1.02-1.05 5 in crystallization by chilling the temperature of the solution is kept at most 12°f below the saturation temperature at the prevailing concentration 6 growth rates of crystals under satisfactory conditions are in the range of 0.10.8 mm/hr the growth rates are approximately the same in all directions 7 growth rates are influenced greatly by the presence of impurities and of certain specific additives that vary from case to case -disintegration1 percentages of material greater than 50 of the maximum size are about 50 from rolls 15 from tumbling mills and 5 from closed circuit ball mills 2 closed circuit grinding employs external size classification and return of oversize for regrinding the rules of pneumatic conveying are applied to design of air classifiers closed circuit is most common with ball and roller mills 3 jaw crushers take lumps of several feet in diameter down to 4 in stroke rates are 100-300/min the average feed is subjected to 8-10 strokes before it becomes small enough to escape gyratory crushers are suited to slabby feeds and make a more rounded product 4 roll crushers are made either smooth or with teeth a 24 in toothed roll can accept lumps 14 in dia smooth rolls effect reduction ratios up to about 4 speeds are 50-900 rpm capacity is about 25 of the maximum corresponding to a continuous ribbon of material passing through the rolls 5 hammer mills beat the material until it is small enough to pass through the screen at the bottom of the casing reduction ratios of 40 are feasible large units operate at 900 rpm smaller ones up to 16,000 rpm for fibrous materials the screen is provided with cutting edges 6 rod mills are capable of taking feed as large as 50 mm and reducing it to 300 mesh but normally the product range is 8-65 mesh rods are 25-150 mm dia ratio of rod length to mill diameter is about 1.5 about 45 of the mill volume is occupied by rods rotation is at 50-65 of critical 7 ball mills are better suited than rod mills to fine grinding the charge is of equal weights of 1.5 2 and 3 in balls for the finest grinding volume occupied by the balls is 50 of the mill volume rotation speed is 70-80 of critical ball mills have a length to diameter ratio in the range 1-1.5 tube mills have a ratio of 4-5 and are capable of very fine grinding pebble mills have

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ceramic grinding elements used when contamination with metal is to be avoided 8 roller mills employ cylindrical or tapered surfaces that roll along flatter surfaces and crush nipped particles products of 20-200 mesh are made -distillation and gas absorption a1 distillation usually is the most economical method of separating liquids superior to extraction adsorption crystallization or others exceptions to this rule include flash separation when flash separation is sufficient and settling decanting or coalescing when the mixture has ll immiscibility without addition of extraction solvent 2 for ideal mixtures relative volatility is the ratio of vapor pressures 12 p2 p1 3 tower operating pressure is determined most often by the temperature of the available condensing medium 100-120 f if cooling water or by the maximum allowable reboiler temperature 150 psig steam 366 f 4 sequencing of columns for separating multicomponent mixtures a perform the easiest separation first that is the one least demanding of trays and reflux and leave the most difficult to the last b when neither relative volatility nor feed concentration vary widely remove the components one by one as overhead products c when the adjacent ordered components in the feed vary widely in relative volatility sequence the splits in the order of decreasing volatility d when the concentrations in the feed vary widely but the relative volatilities do not remove the components in the order of decreasing concentration in the feed 5 economically optimum reflux ratio is about 1.2 times the minimum reflux ratio rm 6 the economically optimum number of trays is near twice the minimum value nm 7 the minimum number of trays is found with the fenske underwood equation nm log x 1 x ovhd x 1 x btms log 8 minimum reflux for binary or psuedobinary mixtures is given by the following when separation is essentially complete xd 1 and d f is the ratio of overhead product and feed rates rmd/f 1 -1 when feed is at the bubblepoint rm 1d/f 1 when feed is at the dewpoint -distillation and gas absorption b1 a safety factor of 10 of the number of trays calculated by the best means is advisable.

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2 reflux pumps are made at least 25 oversize 3 for reasons of accessibility tray spacings are made 20-24 in 4 peak efficiency of trays is at values of the vapor factor fs uv0.5 in the range 1.0-1.2 ft/sec lb/cuft0.5 this range of fs establishes the diameter of the tower roughly linear velocities are 2 ft/sec at moderate pressures and 6 ft/sec in vacuum 5 the optimum value of the kremser-brown absorption factor a kv l is in the range 1.25-2.0 6 pressure drop per tray is of the order of 3 in of water or 0.1 psi 7 tray efficiencies for distillation of light hydrocarbons and aqueous solutions are 60-90 for gas absorption and stripping 10-20 8 sieve trays have holes 0.25-0.50 in dia hole area being 10 of the active cross section 9 valve trays have holes 1.5 in dia each provided with a liftable cap 12-14 caps/sqft of active cross section valve trays usually are cheaper than sieve trays 10 bubblecap trays are used only when a liquid level must be maintained at low turndown ratio they can be designed for lower pressure drop than either sieve or valve trays 11 weir heights are 2 in weir lengths about 75 of tray diameter liquid rate a maximum of about 8 gpm/in of weir multipass arrangements are used at high liquid rates 12 packings of random and structured character are suited especially to towers under 3 ft dia and where low pressure drop is desirable with proper initial distribution and periodic redistribution volumetric efficiencies can be made greater than those of tray towers packed internals are used as replacements for achieving greater throughput or separation in existing tower shells -distillation and gas absorption c1 for gas rates of 500 cfm use 1 in packing for gas rates of 2000 cfm or more use 2 in 2 the ratio of diameters of tower and packing should be at least 15 3 because of deformability plastic packing is limited to a 10-15 ft depth unsupported metal to 20-25 ft 4 liquid redistributors are needed every 5-10 tower diameters with pall rings but at least every 20 ft the number of liquid streams should be 3-5/sqft in towers larger than 3 ft dia some experts say 9-12/sqft and more numerous in smaller towers 5 height equivalent to a theoretical plate hetp for vapor-liquid contacting is 1.3-1.8 ft for 1 in pall rings 2.5-3.0 ft for 2 in pall rings.

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6 packed towers should operate near 70 of the flooding rate given by the correlation of sherwood lobo et al 7 reflux drums usually are horizontal with a liquid holdup of 5 min half full a takeoff pot for a second liquid phase such as water in hydrocarbon systems is sized for a linear velocity of that phase of 0.5 ft/sec minimum diameter of 16 in 8 for towers about 3 ft dia add 4 ft at the top for vapor disengagement and 6 ft at the bottom for liquid level and reboiler return 9 limit the tower height to about 175 ft max because of wind load and foundation considerations an additional criterion is that l/d be less than 30 -drivers and power reocvery equipment1 efficiency is greater for larger machines motors are 85-95 steam turbines are 42-78 gas engines and turbines are 28-38 2 for under 100 hp electric motors are used almost exclusively they are made for up to 20,000 hp 3 induction motors are most popular synchronous motors are made for speeds as low as 150 rpm and are thus suited for example for low speed reciprocating compressors but are not made smaller than 50 hp a variety of enclosures is available from weather-proof to explosion-proof 4 steam turbines are competitive above 100 hp they are speed controllable frequently they are employed as spares in case of power failure 5 combustion engines and turbines are restricted to mobile and remote locations 6 gas expanders for power recovery may be justified at capacities of several hundred hp otherwise any needed pressure reduction in process is effected with throttling valves -drying of solids1 drying times range from a few seconds in spray dryers to 1 hr or less in rotary dryers and up to several hours or even several days in tunnel shelf or belt dryers 2 continuous tray and belt dryers for granular material of natural size or pelleted to 3-15 mm have drying times in the range of 10-200 min 3 rotary cylindrical dryers operate with superficial air velocities of 5-10 ft/sec sometimes up to 35 ft/sec when the material is coarse residence times are 5-90 min holdup of solid is 7-8 4 an 85 free cross section is taken for design purposes in countercurrent flow the exit gas is 10-20°c above the solid in parallel flow the temperature

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5 6 7 8 9 of the exit solid is 100°c rotation speeds of about 4 rpm are used but the product of rpm and diameter in feet is typically between 15 and 25 drum dryers for pastes and slurries operate with contact times of 3-12 sec produce flakes 1-3 mm thick with evaporation rates of 15-30kg/m2hr diameters are 1.5-5.0ft the rotation rate is 2-10 rpm the greatest evaporative capacity is of the order of 3000 lb/hr in commercial units pneumatic conveying dryers normally take particles 1-3 mm dia but up to 10 mm when the moisture is mostly on the surface air velocities are 10-30 m/sec single pass residence times are 0.5-3.0 sec but with normal recycling the average residence time is brought up to 60 sec units in use range from 0.2 m dia by 1 m high to 0.3 m dia by 38 m long air requirement is several scfm/lb of dry product/hr fluidized bed dryers work best on particles of a few tenths of a mm dia but up to 4 mm dia have been processed gas velocities of twice the minimum fluidization velocity are a safe prescription in continuous operation drying times of 1-2 min are enough but batch drying of some pharmaceutical products employs drying times of 2-3 hr spray dryers surface moisture is removed in about 5 sec and most drying is completed in less than 60 sec parallel flow of air and stock is most common atomizing nozzles have openings 0.012-0.15 in and operate at pressures of 300-4000 psi atomizing spray wheels rotate at speeds to 20,000 rpm with peripheral speeds of 250-600 ft/sec with nozzles the length to diameter ratio of the dryer is 4-5 with spray wheels the ratio is 0.5-1.0 for the final design the experts say pilot tests in a unit of 2 m dia should be made -evaporators1 long tube vertical evaporators with either natural or forced circulation are most popular tubes are 19-63 mm dia and 12-30 ft long 2 in forced circulation linear velocities in the tubes are 15-20 ft/sec 3 elevation of boiling point by dissolved solids results in differences of 3-10°f between solution and saturated vapor 4 when the boiling point rise is appreciable the economic number of effects in series with forward feed is 4-6 5 when the boiling point rise is small minimum cost is obtained with 8-10 effects in series 6 in backward feed the more concentrated solution is heated with the highest temperature steam so that heating surface is lessened but the solution must be pumped between stages.

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7 the steam economy of an n-stage battery is approximately 0.8n lb evaporation/lb of outside steam 8 interstage steam pressures can be boosted with steam jet compressors of 2030 efficiency or with mechanical compressors of 70-75 efficiency -extraction liquid-liquid1 the dispersed phase should be the one that has the higher volumetric rate except in equipment subject to backmixing where it should be the one with the smaller volumetric rate it should be the phase that wets the material of construction less well since the holdup of continuous phase usually is greater that phase should be made up of the less expensive or less hazardous material 2 there are no known commercial applications of reflux to extraction processes although the theory is favorable treybal 3 mixer-settler arrangements are limited to at most five stages 2 mixing is accomplished with rotating impellers or circulating pumps settlers are designed on the assumption that droplet sizes are about 150 µm dia in open vessels residence times of 30-60 min or superficial velocities of 0.5-1.5 ft/min are provided in settlers extraction stage efficiencies commonly are taken as 80 4 spray towers even 20-40 ft high cannot be depended on to function as more than a single stage 5 packed towers are employed when 5-10 stages suffice pall rings of 1-1.5in size are best dispersed phase loadings should not exceed 25 gal min sqft hets of 5-10 ft may be realizable the dispersed phase must be redistributed every 5-7 ft packed towers are not satisfactory when the surface tension is more than 10 dyn/cm 6 sieve tray towers have holes of only 3-8 mm dia velocities through the holes are kept below 0.8 ft/sec to avoid formation of small drops redispersion of either phase at each tray can be designed for tray spacings are 6-24 in tray efficiencies are in the range of 20-30 7 pulsed packed and sieve tray towers may operate at frequencies of 90 cycles/min and amplitudes of 6-25 mm in large diameter towers hets of about 1 m has been observed surface tensions as high as 30-40 dyn/cm have no adverse effect 8 reciprocating tray towers can have holes 9/16 in dia 50-60 open area stroke length 0.75 in 100-150 strokes/min plate spacing normally 2 in but in the range 1-6 in in a 30 in dia tower hets is 20-25 in and throughput is 2000 gal hr sqft power requirements are much less than of pulsed towers.

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9 rotating disk contactors or other rotary agitated towers realize hets in the range 0.1-0.5 m the especially efficient kuhni with perforated disks of 40 free cross section has hets 0.2 m and a capacity of 50 m3/m2 hr -filtration1 processes are classified by their rate of cake buildup in a laboratory vacuum leaf filter rapid 0.1-10.0 cm/sec medium 0.1-10.0cm/min slow 0.110.0cm/hr 2 continuous filtration should not be attempted if 1/8 in cake thickness cannot be formed in less than 5 min 3 rapid filtering is accomplished with belts top feed drums or pusher-type centrifuges 4 medium rate filtering is accomplished with vacuum drums or disks or peelertype centrifuges 5 slow filtering slurries are handled in pressure filters or sedimenting centrifuges 6 clarification with negligible cake buildup is accomplished with cartridges precoat drums or sand filters 7 laboratory tests are advisable when the filtering surface is expected to be more than a few square meters when cake washing is critical when cake drying may be a problem or when precoating may be needed 8 for finely ground ores and minerals rotary drum filtration rates may be 1500 lb day sqft at 20 rev/hr and 18-25 in hg vacuum 9 coarse solids and crystals may be filtered at rates of 6000 lb day sqft at 20rev/hr 2-6 in hg vacuum -fluidization of particles with gases1 properties of particles that are conducive to smooth fluidization include rounded or smooth shape enough toughness to resist attrition sizes in the range 50-500 µm dia a spectrum of sizes with ratio of largest to smallest in the range of 10-25 2 cracking catalysts are members of a broad class characterized by diameters of 30-150 µm density of 1.5 g/ml or so appreciable expansion of the bed before fluidization sets in minimum bubbling velocity greater than minimum fluidizing velocity and rapid disengagement of bubbles 3 the other extreme of smoothly fluidizing particles is typified by coarse sand and glass beads both of which have been the subject of much laboratory investigation their sizes are in the range 150-500 µm densities 1.5-4.0 g/ml small bed expansion about the same magnitudes of minimum bubbling and minimum fluidizing velocities and also have rapidly disengaging bubbles.

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4 cohesive particles and large particles of 1 mm or more do not fluidize well and usually are processed in other ways 5 rough correlations have been made of minimum fluidization velocity minimum bubbling velocity bed expansion bed level fluctuation and disengaging height experts recommend however that any real design be based on pilot plant work 6 practical operations are conducted at two or more multiples of the minimum fluidizing velocity in reactors the entrained material is recovered with cyclones and returned to process in dryers the fine particles dry most quickly so the entrained material need not be recycled -heat exchangers1 take true countercurrent flow in a shell-and-tube exchanger as a basis 2 standard tubes are 3/4 in od 1 in triangular spacing 16 ft long a shell 1 ft dia accommodates 100 sqft 2 ft dia 400 sqft 3 ft dia 1100 sqft 3 tube side is for corrosive fouling scaling and high pressure fluids 4 shell side is for viscous and condensing fluids 5 pressure drops are 1.5 psi for boiling and 3-9 psi for other services 6 minimum temperature approach is 20°f with normal coolants 10°f or less with refrigerants 7 water inlet temperature is 90°f maximum outlet 120°f 8 heat transfer coefficients for estimating purposes btu hr sqft °f water to liquid 150 condensers 150 liquid to liquid 50 liquid to gas 5 gas to gas 5 reboiler 200 max flux in reboilers 10,000 btu hr sqft 9 double-pipe exchanger is competitive at duties requiring 100-200 sqft 10 compact plate and fin exchangers have 350 sqft/cuft and about 4 times the heat transfer per cuft of shell-and-tube units 11 plate and frame exchangers are suited to high sanitation services and are 25-50 cheaper in stainless construction than shell-and-tube units 12 air coolers tubes are 0.75-1.00in 00 total finned surface 15-20 sqft/sqft bare surface u 80-100 btu hr sqft bare surface °f fan power input 2-5 hp mbtu/hr approach 50°f or more 13 fired heaters radiant rate 12,000 btu hr sqft convection rate 4000 cold oil tube velocity 6 ft/sec approx equal transfers of heat in the two sections thermal efficiency 70-75 flue gas temperature 250-350°f above feed inlet stack gas temperature 650-950°f -insulation1 up to 650°f 85 magnesia is most used 2 up to 1600-1900°f a mixture of asbestos and diatomaceous earth is used.

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3 ceramic refractories at higher temperatures 4 cyrogenic equipment 200°f employs insulants with fine pores in which air is trapped 5 optimum thickness varies with temperature 0.5 in at 200°f 1.0in at 400°f 1.25 in at 600°f 6 under windy conditions 7.5 miles/hr 10-20 greater thickness of insulation is justified -mixing and agitation1 mild agitation is obtained by circulating the liquid with an impeller at superficial velocities of 0.1-0.2 ft/sec and intense agitation at 0.7-1.0ft/sec 2 intensities of agitation with impellers in baffled tanks are measured by power input hp/1000 gal and impeller tip speeds 0peration hp /1000 gal tip speed ft/min blending 0.2-0.5 homogeneous reaction 0.5-1.5 7.5-10 reaction with heat transfer 1.5-5.0 10-15 liquid-liquid mixtures 5 15-20 liquid-gas mixtures 5-10 15-20 slurries 10 3 proportions of a stirred tank relative to the diameter d liquid level d turbine impeller diameter d/3 impeller level above bottom d/3 impeller blade width d/15 four vertical baffles with width d/10 4 propellers are made a maximum of 18 in turbine impellers to 9 ft 5 gas bubbles sparged at the bottom of the vessel will result in mild agitation at a superficial gas velocity of 1 ft/min severe agitation at 4 ft/min 6 suspension of solids with a settling velocity of 0.03 ft/sec is accomplished with either turbine or propeller impellers but when the settling velocity is above 0.15 ft/sec intense agitation with a propeller is needed 7 power to drive a mixture of a gas and a liquid can be 25-50 less than the power to drive the liquid alone 8 in-line blenders are adequate when a second or two contact time is sufficient with power inputs of 0.1-0.2 hp/gal -particle size enlargement1 the chief methods of particle size enlargement are compression into a mold extrusion through a die followed by cutting or breaking to size globulation of molten material followed by solidification agglomeration under tumbling or otherwise agitated conditions with or without binding agents.

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2 rotating drum granulators have length to diameter ratios of 2-3 speeds of 1020 rpm pitch as much as 10° size is controlled by speed residence time and amount of binder 2-5 mm dia is common 3 rotary disk granulators produce a more nearly uniform product than drum granulators fertilizer is made 1.5-3.5 mm iron ore 10-25 mm dia 4 roll compacting and briquetting is done with rolls ranging from 130 mm dia by 50 mm wide to 910 mm dia by 550 mm wide extrudates are made 1-10 mm thick and are broken down to size for any needed processing such as feed to tabletting machines or to dryers 5 tablets are made in rotary compression machines that convert powders and granules into uniform sizes usual maximum diameter is about 1.5 in but special sizes up to 4 in dia are possible machines operate at 100 rpm or so and make up to 10,000 tablets/min 6 extruders make pellets by forcing powders pastes and melts through a die followed by cutting an 8 in screw has a capacity of 2000 lb/hr of molten plastic and is able to extrude tubing at 150-300 ft/min and to cut it into sizes as small as washers at 8000/min ring pellet extrusion mills have hole diameters of 1.6-32 mm production rates cover a range of 30-200 ib hr hp 7 frilling towers convert molten materials into droplets and allow them to solidify in contact with an air stream towers as high as 60 m are used economically the process becomes competitive with other granulation processes when a capacity of 200 400 tons/day is reached ammonium nitrate prills for example are 1.6-3.5 mm dia in the 5-95 range 8 fluidized bed granulation is conducted in shallow beds 12-24 in deep at air velocities of 0.1-2.5 m/s or 3-10 times the minimum fluidizing velocity with evaporation rates of 0.005 1.0 kg/m2 sec one product has a size range 0.72.4 mm dia -piping1 line velocities and pressure drops with line diameter d in inches liquid pump discharge 5 d /3 ft/sec 2.0 psi/100 ft liquid pump suction 1.3 d /6 ft/sec 0.4 psi/100 ft steam or gas 20d ft/sec 0.5 psi/100 ft 2 control valves require at least 10 psi drop for good control 3 globe valves are used for gases for control and wherever tight shutoff is required gate valves are for most other services 4 screwed fittings are used only on sizes 1.5 in and smaller flanges or welding otherwise 5 flanges and fittings are rated for 150 300 600 900 1500 or 2500 psig.

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6 pipe schedule number 1000p/s approximately where p is the internal pressure psig and s is the allowable working stress about 10,000 psi for a120 carbon steel at 500°f schedule 40 is most common -pumps1 power for pumping liquids hp gpm psi difference 1714 fractional efficiency 2 normal pump suction head npsh of a pump must be in excess of a certain number depending on the kind of pumps and the conditions if damage is to be avoided npsh pressure at the eye of the impeller vapor pressure density common range is 4-20 ft 3 specific speed ns rpm gpmo.s head in ft0.75 pump may be damaged if certain limits of ns are exceeded and efficiency is best in some ranges 4 centrifugal pumps single stage for 15-5000 gpm 500 ft max head multistage for 20-11,000 gpm 5500 ft max head efficiency 45 at 100 gpm 70 at 500 gpm 80 at 10,000 gpm 5 axial pumps for 20-100,000 gpm 40 ft head 65-85 efficiency 6 rotary pumps for 1-5000 gpm 50,000 ft head 50-80 efficiency 7 reciprocating pumps for 10-10,000 gpm 1,000,000 ft head max efficiency 70 at 10 hp 85 at 50 hp 90 at 500 hp -reactors1 the rate of reaction in every instance must be established in the laboratory and the residence time or space velocity and product distribution eventually must be found in a pilot plant 2 dimensions of catalyst particles are 0.1 mm in fluidized beds 1 mm in slurry beds and 2-5 mm in fixed beds 3 the optimum proportions of stirred tank reactors are with liquid level equal to the tank diameter but at high pressures slimmer proportions are economical 4 power input to a homogeneous reaction stirred tank is 0.5-1.5 hp/1000 gal but three times this amount when heat is to be transferred 5 ideal cstr continuous stirred tank reactor behavior is approached when the mean residence time is 5-10 times the length of time needed to achieve homogeneity which is accomplished with 500-2000 revolutions of a properly designed stirrer 6 batch reactions are conducted in stirred tanks for small daily production rates or when the reaction times are long or when some condition such as feed rate or temperature must be programmed in some way 7 relatively slow reactions of liquids and slurries are conducted in continuous stirred tanks a battery of four or five in series is most economical.

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