WO1999064356A1 - Systeme de traitement - Google Patents

Systeme de traitement Download PDF

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Publication number
WO1999064356A1
WO1999064356A1 PCT/US1999/013405 US9913405W WO9964356A1 WO 1999064356 A1 WO1999064356 A1 WO 1999064356A1 US 9913405 W US9913405 W US 9913405W WO 9964356 A1 WO9964356 A1 WO 9964356A1
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WO
WIPO (PCT)
Prior art keywords
solvent
separator
membrane
liquor
stream
Prior art date
Application number
PCT/US1999/013405
Other languages
English (en)
Other versions
WO1999064356A9 (fr
Inventor
Leon J. Potter
Original Assignee
Hensley, Gary, L.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US09/099,166 external-priority patent/US5997652A/en
Priority claimed from US09/187,239 external-priority patent/US6177014B1/en
Priority claimed from US09/260,745 external-priority patent/US6155964A/en
Application filed by Hensley, Gary, L. filed Critical Hensley, Gary, L.
Priority to AU46827/99A priority Critical patent/AU4682799A/en
Publication of WO1999064356A1 publication Critical patent/WO1999064356A1/fr
Publication of WO1999064356A9 publication Critical patent/WO1999064356A9/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
    • C08B30/00—Preparation of starch, degraded or non-chemically modified starch, amylose, or amylopectin
    • C08B30/04—Extraction or purification
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/06—Tubular membrane modules
    • B01D63/062—Tubular membrane modules with membranes on a surface of a support tube
    • B01D63/063—Tubular membrane modules with membranes on a surface of a support tube on the inner surface thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/02—Inorganic material
    • B01D71/024—Oxides
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B21/00—Methods or apparatus for flushing boreholes, e.g. by use of exhaust air from motor
    • E21B21/06—Arrangements for treating drilling fluids outside the borehole
    • E21B21/063—Arrangements for treating drilling fluids outside the borehole by separating components

Definitions

  • the kernel is processed typically by cooking to soften the kernel.
  • the corn is at least separated from the shuck, and the kernels are removed from the corn cob. Thereafter, they may be processed by any number of subsequent cooking procedures. By crushing, corn starch can be derived. By appropriate pre-treatment and subsequent cooking, the corn can be converted into hominy. The foregoing is also true of rice in that it has to separated from the husk and subsequently cooked.
  • waste discharge is a water stream which carries in it some pulp from the processed fruit, vegetables and grain so that the treatment throws away a portion of the unconverted feed (the picked and ready to treat fruit, vegetable or grain).
  • the husk or hull is removed and is salvaged. It is obtained in a dry state.
  • the next step of treatment involves cooking the rice. It is cooked in water and subsequently separated from that water.
  • the water stream includes a very significant portion of starch or sugar derivatives. These are normally carried in suspension although a portion of it will dissolve into the water. It leaves a very difficult waste stream to handle. It is difficult to separate out any sediment in light of the volume is handled. Through the use of settling tanks, some portions can be removed, but the bulk of the food components remain suspended or dissolved in the waste water stream.
  • the waste water is typically delivered at an elevated temperature. That tends to increase the amount entering into solution.
  • the present disclosure sets out a method and apparatus for improved and enhanced treatment of food processing plant streams. It is particularly intended for use with those plants processing grains, fruit and vegetables. It is especially effective in the treatment of heated waste streams which are laden with bits of pulp, shredded skin (as would occur in an apple processing plant) and can recover components of substantial value.
  • An example will be given below referring to a rice processing plant.
  • the plant cooks the rice in water for a specified interval at elevated temperatures and then continues to treat the rice kernel after removing the kernel from the hot water.
  • the hot water stream (otherwise a waste product stream) is input to a system for improving the post cooking treatment of the spent hot liquor using that term to apply to the waste water laden with pieces of the grain, fruit or vegetable either in solution or in suspension or both.
  • the waste stream is delivered to a processing plant in which the water is ' extracted for easy disposal.
  • the stream of water after treatment places minor demands on the sewage system.
  • This water is clarified and otherwise stripped of the derivatives from the fruit, vegetable or grain treated in the plant.
  • the input will be termed the "liquor” and the liquor is broken down into two components by the treatment process and is discharged as the clarified solvent (practically always water) while the recovered components will be described generally as the extract.
  • the extract is comprised of some pulp from the liquor and includes a significant portion of starches and sugars.
  • the present method and apparatus are summarized as a disposal system for food processing plant to handle the discharged liquor from the process.
  • This stream which is otherwise wasted includes the solvent and relatively valuable food components which are recovered.
  • This recovery approach uses a combination membrane filtration in conjunction with centrifuge separation.
  • the recovery is markedly enhanced by combining the two procedures in conjunction with a feedback flow so that reprocessing is carried out in a continuous fashion, and the achieved results are controllably executed in a combined system .
  • a control system is implemented so that the flow of the food plant liquor is appropriately processed to make this valuable recovery.
  • the discharged water from this process is more easily disposed, and is not laden with the excessive food plant components which otherwise have such a high oxygen demand in subsequent processing as sewage.
  • the starch and pulp provided by a fruit, grain or root related material processed after harvesting for easy consumption or digestion varies significantly. For instance, the pacific rim region of the world places a great deal of emphasis on rice. It is a major staple of life, and is manufactured into rice related prices in great quantity.
  • Rice is a food product forming a starch which is somewhat different than any other starch. When rice is cooked and a portion of the kernal is converted into starch, this starch has a significantly different physical characteristic than the starch from other comprable plants.
  • the granuals of rice starch are quite small, typically in the range of about 3 to about 8 microns maximum diameter, and the meduim appears to be around 4 or perhaps 5 microns.
  • the processing of rice therefore requires careful construction of the porous membrane involved in the separation process as will be detailed below.
  • the rice starch molecules are granules at that small size can be segregated based on granule size. This makes a significant impact in the processing and separation. Even where some water of hydrate is absorbed, and the granules agglomerate, the granules can be segregated more readily taking advantage of this small size. Effectively, this means that rice particles from a food processing plant should be kept separate and can be processed taking advantage of the relative small granule size.
  • Potatoes have a swelling power of in excess of 1 ,000. This is a significant difference in comparison with the swelling power of wheat (about 21 ) or tapioca, a swelling power of about 70, to compare a similar root based product. Not only that, but this starch from potatoes has a very high solubility of about 80%, well above the solubility levels of about 20% to about 48% for other items (tapioca being the closest). This helps identify and distinguish the processed starch products obtained from processing plant liquor dealing in potatoes .
  • STARCH Starch is a carbohydrate, composed of carbon, hydrogen, and oxygen atoms in the ratio 6 : 10 : 5, (C6H ⁇ o ⁇ 5 )n.
  • Starch can be considered a condensation polymer of glucose, consisting of anhydroglucose units.
  • the glucose units are linked to one another through the Cl oxygen, known as glucoside bond.
  • the glucoside linkage is stable under alkaline conditions and hydrolyzable under acid conditions.
  • the glucose unit at the end of the polymeric chain has a latent aldehyde group and is know as the reducing end group.
  • starches are a mixture of amylose and amylopectin, each with a wide range of molecular sizes.
  • Thomas Schoch demonstrated the fractionation of starch by adding butanol to a starch solution. Butanol formed an insoluble crystalline complex with the amylose traction. Starches of different origin have different amylose-amylopectin ratios, as the Table 1 shows. Both fractions in various starches are highly polymerized.
  • Amylose and amylopectin contents and degree of polymerization of various starches are developed below.
  • Table 2 shows the tendency of the starches to gelatinize.
  • Table 3 shows very little difference in various starches in terms of chemical make up.
  • RH relative humidity.
  • t>DS dry substance.
  • C N nitrogen content.
  • Table 4 lists some granulation differences. These overlap greatly.
  • Table 5 shows some difference in moisture content at the unprocessed stage, but some dry weight differences do exist, albeit they are small differences.
  • cooking leads to the formation of physical or chemical complexes between starch and other materials, e.g. fat or proteins.
  • Such complexes may be resistant to attack by amylolytic enzymes and this "resistant starch" is an area of current interest in relation to definitions and measurements of dietary fiber.
  • some starch complexes which are resistant in the in vitro enzyme systems used in some methods of dietary fiber analysis are, in fact, digested in vivo to the same extent, albeit less rapidly, as the uncomplexed, cooked starch.
  • digestibility of starch is, to some extent, dependent upon the botanical source and type of cooking. For example, extrusion-cooking of flour can give greater digestibility of starch than does conventional cooking. Placing selected data in tabular form, one recognizes the re-arranged data, thusly: Table 6.
  • Table 1 shows that there is very little basis for discrimination based on the relative weight percent of amylose compared with the amylopectin.
  • Table 2 shows that there is very little prospect of distinguishing rice starch molecules as set forth in Table 1 , and the same is really of the data found in Table 2. It is, however, possible to obtain some slight benefit from the data in Table 3, provided one is willing to go into other kinds of tests.
  • Moisture content test however, require the kind of laboratory diagnostic equipment that is difficult to implement.
  • the average size of the starch molecule is assisted tremendously by the data set forth in Table 4. There, it will be observed that rice is the smallest average diameter. It shows a diameter of about 5 microns; by contrast, other molecules are just simply bigger.
  • the molecular pore through the membrane have a size that does not pass the average rice starch granule.
  • a pore size of about 1 to 3 microns. If desired, the largest pore is about 2 microns.
  • Table 5 shows some difference in the moisture content at the unprocessed stage. As will be observed, there is a difference in the moisture content dependent of the feedstock. Here, there is little differentiation between rice and wheat, but that differentiation can be enhanced by working with a molecular pore size of the sort just given. Finally, it will be observed in Table 6 that the medium size of corn and wheat are perhaps closer, but that can be distinguished notably by use of a small pore to separate rice starch granules.
  • the present method is summarized as a disposal method for rice processing plant to handle the discharged liquor from the process.
  • This stream which is otherwise wasted includes the water solvent and relatively valuable food components which are recovered.
  • This recovery approach uses a membrane filtration in conjunction with centrifuge separation.
  • the recovery is markedly enhanced by serially combining the procedures in conjunction with a feedback flow so that reprocessing is carried out in a continuous fashion, and the achieved results are controllably executed in a combined system.
  • a control system is implemented so that the flow of the rice plant liquor is appropriately processed to make this valuable recovery.
  • the discharged water from this process is more easily disposed, and is not laden with the excessive food plant components which otherwise have such a high oxygen demand in subsequent processing as sewage.
  • drilling mud In drilling an oil well, the drill bit is normally lubricated with a flow of drilling mud.
  • the initial drilling fluid in general terms is known as drilling mud.
  • drilling muds Over the years, drilling muds have evolved into rather sophisticated mixtures.
  • the basic solvent usually is water but enhanced solvents are known and will be discussed below.
  • the drilling mud has weight components added. Generally these are clay related item which are relatively slick in the water.
  • the weight materials normally include barites which are added for weight.
  • the composite weight of the drilling mud can be increased from a nominal 8.5 pounds per gallon (that of water) to heavier weights, even as much as double that. A fifteen pound mud is often used to enhance the hydrostatic pressure of the mud in the well.
  • the solvent water carries a large volume of barites and other clay related products in it. Commonly these dissolve in small measure but they are primarily sedimentary suspensions.
  • the mud is recycled at the surface through a variety of processes and is continually used during drilling. Usually, it becomes so heavily laden with formation particles that it has to be purified continuously. Otherwise, it loses its desired characteristics.
  • the drilling mud solvent is changed from water to oil, oil typically having the weight or consistency of diesel oil.
  • the incline of the well is determined by the incline of the formation i.e. the dip or position of the formation in the earth. Accordingly, the deviated well portion will extend horizontally (where the formation has no dip) or might incline downwardly at 20° where the formation has a dip of 20° in that direction.
  • Drilling in these formations requires a different kind of mud system. These mud systems typically require an expensive oil for the solvent. Once, these were known as "palm oil” even though they are not necessarily derived from palm trees. Whether palm oil or some synthetic having a similarity to that, these wells have been drilled using oils costing as much as $300 per barrel. This is significantly more expensive than the more common solvents, namely diesel oil or water.
  • the mud system is significantly expensive.
  • the weight material added to the expensive oil comprises a number of organic systems typified by starches. These have the form of relatively heavy molecules which have a desired cohesive reaction.
  • the weight material form a filtrate cake against the side wall. Heavier weight materials are used at this stage, and dynamic pressure in the well borehole is equal to and preferably somewhat greater than the formation pressure. This prevents the formation from producing while drilling the incomplete well borehole. Further, this keeps the formation on the other side of the filtrate formed of starches.
  • the filtrate forms a desirable barrier which is pressure actuated so that formation isolation is obtained, loss of solvent is reduced, and drilling continues on the inside of the filtrate cake, thereby enabling evacuation of the drilling particles.
  • the mud cake is left on the side wall and positive pressure is maintained against it.
  • the next stage of the drilling procedure typically involves the insertion of either a screen or a slotted casing which effectively serves as a screen.
  • the screen or casing props the hole open so that it does not collapse with production. There is a likelihood of collapse of the hole i.e. it may cave in. By maintaining positive pressure, this likelihood is reduced.
  • the screen or slotted casing is perforated so that enough openings are provided that the formation can produce into it. In a typical vertical well, perforations are formed only at the producing zone. The perforations form radially extending openings out into the formation through the casing and cement around the casing.
  • the screen or slotted casing is installed first and subsequent treatments are undertaken to increase the amount of formation exposed for production units the well borehole.
  • the next step typically involves at least washing the well to open up the formation pores, and often involves hydraulic fracture or acid treatment to eat away some portion of the formation to thereby increase flow from the formation into the well borehole.
  • a measured quantity of hydraulic oil is pumped into the formation and is forced through the screen out into the formation. The pressure is raised so that cracks and fissures are formed in the formation. If need be, the cracks are held open by mixing a proppant material in the oil.
  • the proppant typically is small beads or other particles which are distributed into the formation at cracks formed by hydraulic pressure to widen the cracks.
  • the acid is delivered under pressure into the formation so that the formation is partly eaten away. This typically preferentially attacks some component of the formation but not the whole formation.
  • the acid typically will preferentially attack the sand and thereby increase the pore size in the formation, thereby increasing flow through the enlarged pores. The formation will flow more readily after acid treatment.
  • the discharge (obviously one phase of drilling activities) will at different times include the various components just mentioned.
  • the heavy molecule starch components will be discharged.
  • drilling mud as used below will refer to any of the additives incorporated with a drilling fluid.
  • solvent will refer to any of the most common solvents which includes conventional water, diesel oil, and synthetic oil sometimes known as “palm oil”.
  • weight material will refer in some instances to barites, or many other instances refer to heavy salts which are added to the drilling fluid.
  • organic additives will refer to the typical drilling fluid constituents such as starches and other heavy molecules. These are typically and commonly added so that a heavy molecule is place in the system and yet is soluble with the solvent.
  • the heavy molecule increases the weight of the filtrate, and also functions as a filtrate which reduces formation production at the initial stages prior to lining the well with a screen or slotted production casing. All of these when retrieved have value. Retrieval, however, is sometimes difficult. That problem will be developed below.
  • This disclosure is directed to a portable system which is adapted for use with a set of mud tanks of the sort normally found at a drilling rig. More particularly, the system enables portable field treatment of the drilling mud and other completion fluids which recovers the cuttings, weight materials, organics and segregates the solvent. This enables the solvent to be used repetitively. The solvent can be then sent to another rig site, or recycled in the drilling process. The cuttings and other additives are selectively removed. This enables a less costly disposal process to be undertaken. For instance if the well is a developmental well in a field that has already been discovered, there will typically be an injection formation available where the cuttings for that particular well can be injected back through another well drilled into the same or similar formations.
  • Such disposal wells are usually permitted by regulatory authorities so that cuttings and salt water from that region are returned into formations common to that region.
  • the equipment of the present disclosure enables cleaning for recirculation. This permits an extended life to the mud and fluid schedule and thereby reduces drilling costs.
  • this system especially is advantagous in that operating points of the various equipment can be adjusted to change the separation that are accomplished. These adjustments enable a combination of different solids in the stream to be segregated and recovered.
  • FIG. 1 is a schematic block diagram of a food plant in accordance with the teachings of present disclosure incorporating an input pump connected with a membrane separator operating with a disk centrifuge and incorporating a feedback flow path;
  • Figure 2 is a side view of a membrane separator having the form of an elongate bundle of pipes in a collection sleeve mounted on a trailer;
  • Figure 3 is a view of the truck mounted equipment shown in Fig. 2 showing connections for that equipment;
  • Figure 4 is a simplified view of a single membrane pipe in the apparatus shown in Fig. 2;
  • Figure 5 is a sectional view through the wall of the membrane showing how the membrane segregates the solvent from the particles in the solvent;
  • Figure 6 is an alternate multiple stage centrifuge arrangement in conjunction with a membrane separator to provide more processing
  • Figure 7 is a schematic block diagram of another system
  • Figure 8 shows a graph of membrane length and depicts the improved centrifuge removal of certain mud system components
  • Fig. 9 shows another system.
  • Fig. 1 of the drawing Attention is directed to Fig. 1 of the drawing where the numeral 10 identifies the present apparatus. It is connected to a food plant 12 which delivers a flow of liquor to a tank 14.
  • the tank 14 receives and stores a portion of the liquor to smooth out irregularities in flow. Effectively, it is a surge pond. Ideally, the dwell time in the tank is relatively short. Otherwise, heat will be lost. It may be desirable to insulate the tank so that heat loss does not occur.
  • the tank is connected through an output valve and then to a pump 16.
  • the pump 16 delivers through a feed line 18 into a tank 20 or an alternate tank 22.
  • the line 18 will be described as the input line while line 24 is the feedback line. The cooperation of the feedback line with the tanks and other components will be noted in some detail.
  • the tank 22 has an output connected with a pump 26 and a comparable pump 28 delivers the output of the tank 22.
  • These two tanks, associated pumps, and other lines deliver the liquor for process through a disk centrifuge 30 and a membrane separator 32.
  • the membrane separator is provided with a recirculation pump 34. The operation of this pump will be more readily understood in conjunction with detailed drawings of the membrane separator 32.
  • the system incorporates a method of processing which delivers the feed in the line 18 to the tank 20.
  • the feed line 18 is input to the tank 22.
  • the first processing step is through the membrane separator 32.
  • the feed is input to the tank 22 and therefore is input to the centrifuge 30.
  • the lines which are connected to fill the tanks 20 and 22.
  • Both tanks are similar in that they are equipped with level controllers. Both tanks are also preferably heated.
  • heat can be provided with a heat exchanger or they can also be provided with a steam heated jacket which is connected to a suitable source of steam.
  • the pumps 26 and 28 remove the accumulated tank stored liquor.
  • each tank is equipped with a feedback line from the pump back into the tank to continue stirring the liquor in the tank.
  • the tanks are output through the pumps as illustrated and the pumps deliver the pressure boosted flow input to the membrane separator 32 and the disk centrifuge 30.
  • the membrane separator 32 flows the liquor through an elongate tubular membrane.
  • the membrane is provided with pores through the wall of the membrane. It is preferably made of sintered stainless steel particles which are compacted to define the thickness of the wall.
  • the sintered particles define a plurality of small pores which flow the solvent through the wall.
  • the solvent water in practically every instance
  • the pores are micron size.
  • Collectively, the pores describe a specified or mean pore diameter.
  • the pore diameter can be specified to 100 microns, 10 microns, 1 micron, and even smaller if desired.
  • the pore diameter is selected so that the pores will pass the solvent. This means that the water molecule is sufficiently small that it can flow through the pores.
  • the molecules of the other materials in the liquor are larger and sufficiently large that they do not readily pass through the pores.
  • solutions involving molecules that are sufficiently small will pass through the pores. Particles and molecules above a certain size will not pass through the pores in the membrane.
  • the membrane separator is constructed and arranged so that the pores reject large molecules and particles. For instance, food pulp particles are so large that they will not pass through the pores.
  • the membrane separator takes advantage of this. As the liquor flows through the membrane separator having the form of a porous wall tube (details are set forth below), the water weeps through the wall and collects on the outside of the membrane tube. It is then easily removed. This increases the concentration of the liquor flowing through the membrane tube.
  • the membrane concentrate discharge is directed to the tank 22. It is ultimately input under pressure by the pump 28 to the disk centrifuge 30.
  • the disk centrifuge 30 separates the liquor into two streams. Just as the membrane separator provided this separation, the centrifuge also provides this separation. Without being categorical about the matter, the centrifuge makes a separation based on weight which in this specific instance assists in segregation of the valuable components from the solvent. More specifically, the weight material in the liquor is extracted and removed. It is removed for subsequent use because it has great value.
  • the membrane removes the water which is a relatively small and light weight molecule. It is light weight in the sense that the liquor is a mix of components, some in solution, and some in suspension in the water. So, the membrane 32 removes water making a more highly concentrated liquor which is then cycled through the centrifuge to remove the heavier components i.e. those that are separated by centrifical forces. The enhanced recovery will be developed in some detail below.
  • the feed is derived from processing rice and comprises a flow of hot water perhaps 175°F, dissolved starch i.e. starch and related compounds which have entered into solution, suspensions of starch molecules which effectively become medium size or perhaps even larger molecules held in suspension, typically having substantial bonds to hydrate complexes i.e. water, and larger particles which are chips or dust from the husk, kernel, and other protein or fiber based components in the rice.
  • hydrate complexes i.e. water
  • larger particles which are chips or dust from the husk, kernel, and other protein or fiber based components in the rice.
  • all of the components which are carried in the liquor are not notably dense.
  • they comprise fibrous materials and are distinctly open celled, there will be a substantial hydrate component.
  • starch and starch related products comprise a gelatinous mass of a semi - solid consistency. It has significant and great value.
  • the discharge of water with reduced oxygen demand in disposal is note worthy. In effect, the water is ready to be thrown away and has trivial value, but at least it is more or less easily disposed of without substantial sewage cost and premiums in disposal.
  • the gelatinous mass which is discharged has great value because it can be recycled in a number of ways, for example, by addition to cattle feed and the like. It is also quite suitable for human consumption and can be added as a stiffening agent to other food stuffs. A number of benefits of this will be noted below on review of the extraction apparatus considered in greater detail.
  • the membrane separator 32 is shown for mobile application where it is mounted on a trailer 36 which is towed to a field location and then left. A fixed plant can omit the trailer.
  • the membrane separator comprises a plurality of U-shaped tubes in a surrounding housing or jacket. The jacket captures the clarified discharged solvent.
  • Fig. 4 of the drawings There, the jacket 38 is shown enclosing a U-shaped membrane tube 40.
  • the jacket connects to a header plate 42 at one end and a comparable header 44 at the opposite end.
  • the membrane tube 40 connects with a U-shaped bend 46 at the remote end.
  • the bend 46 is typically made of a nonporous metal such as stainless steel. Generally, that is chemically inert and is not impacted by any fluid flowing through the system.
  • the headers 42 and 44 are included to align a nest of tubes. All the tubes in the nest are made of porous membrane material. There may be several hundred linear segments inside the jacket 38 that serves as a collection vessel.
  • the filtrate which is clarified by the membrane flows through the wall. It is permitted to drip or flow out through the openings 48 at spaced locations.
  • the laden plant liquor is pumped into the U- shaped tube 40 and flows along the tube.
  • the length of the tube is materially shortened by folding it into the two illustrated parts.
  • a serpentine flow path of 2, 4, 6... or more segments is constructed. Assume for example that the feed flows through 20 membrane tubes segments. In this flow path, the flowing solvent has the opportunity to pass through the wall of the membrane tube. It drips downwardly and flows out through the drain 48 in the jacket.
  • the jacket 38 is thus formed of a non permeable material, and is provided with multiple drain ports or openings 48 to remove the discharged filtrate.
  • the membrane which defines the tube 40 is specially constructed. In general terms, it is made with two layers.
  • the wall is made from stainless steel particles which were packed to a particular shape and then joined together by sintering. When sintered, this forms a porous membrane.
  • the pores in the membrane have a specified median diameter.
  • the interior surface is smoothed somewhat by placing a second coating over it. Going to Fig. 5 of the drawings, the sintered stainless steel particles 5 0 comprise the greater portion of the wall thickness.
  • a thin layer of Ti02 powder is placed on the inside surface and likewise sintered to form the layer 52. It provides a more smooth surface and defines the typical or average pore diameter. In this particular instance, the pore diameter for this embodiment is about 0.1 micron.
  • the solvent passes readily through the membrane, the solvent typically being water. Sugars and salts which are dissolved in the solvent typically will also pass through the membrane. As it flows through, it leaves a more and more strong concentration of the light weight particles which remain after the centrifuged removal. This will be defined as the membrane concentrate. In effect, it is all the pulp or solids that remains in the flow. This forms the discharge stream from the separation.
  • the jacket 38 is inclined at an angle. It is equipped with a collection line 54 which is connected to one or more drain points along the jacket 38.
  • an input line 56 is provided for the system. It connects to the end located manifold 58.
  • the manifold 58 also houses the connections for the outlet line 60.
  • the input is delivered into the manifold so that flow is directed into numerous U-shaped membrane tubes exemplified in Fig. 4. They are serially or parallel connected as needed in the manifold 58.
  • the cross sectional flow path for the inlet line 56 is approximately matched by the aggregate cross sectional flow path of the membrane tubes 40. In other words, it is not necessary to restrict flow with the membrane tube 40 . Indeed, relatively smooth laminar flow through the membrane tube 40 is generally desirable.
  • Pressure drop across the membrane tube is relatively nominal. It is desirable that the flow rate be kept to specified velocity. A change in flow rate changes the manner in which the concentrate tends to blind the membrane.
  • the membrane is collectively an elongate filter surface. It is a filter surface which runs the risk of blinding.
  • the concentrate is pumped at a specified at a minimum velocity, and even greater velocities are achieved. This suggests a flow velocity at least above about 14 feet per second velocity along the membrane tube. If insufficient filtration is accomplished, then the tube 40 is simply made longer. That can be done by arranging more tubes in series. As exemplified in Fig. 4, there are two tubes in series. This can be extended to 4, 6, 8 and so on.
  • the number of passes through the membrane tubes is increased so that the optimum amount of solvent is retrieved from the concentrate.
  • the concentrate represents the food stuffs. It is that portion which is later used i.e. appropriate conversion techniques must be applied to it.
  • the flowing concentrate is kept at a adequate velocity to assure that the concentrate does not simply settle against the wall or the tube 40 and thereby blind the tube.
  • the inlet line 56 is also shown in conjunction with a pump 62.
  • the pump 62 assures that there is an adequate velocity through the membrane tube 40.
  • the outlet line 60 is input to a valve 64. Some portion of the concentrate is controllably returned to the inlet line 56 . This enables continuous recycling of the concentrate stream so that appropriate filtering is carried out.
  • the valve 64 divides the outlet, thereby providing a discharge at one branch and a portion for feedback at the other branch.
  • Notable operating parameters include the velocity, pressure and temperature of the fluid system undergoing treatment.
  • the flow velocity is typically kept between about 14 and 16 feet per second in the membrane tube 40.
  • the temperature is typically set between 180°F and 200°F.
  • the input pressure to the membrane tube is in the range of about 150 to 250 psi.
  • the solvent is water
  • the set points are adjusted and the velocity is typically in the range of about 14 to 17 feet per second
  • the temperature is between about 140 and 180 degrees
  • the pressure input to the membrane tube 40 is about 200 psi.
  • the input pressure is kept sufficiently high and the velocity is also kept sufficiently high that the concentrate stream discharge rate is relatively high, i.e., a drop in flow velocity is generally avoided.
  • the disk centrifuge extractor 30 comprises a system having a set of parallel plates which rotate in a pond. By imposing a number of tapered disks in the pond, the disk is able to provide a relatively large surface area pond of relatively shallow depth. Pond depth is related to the transit time. When a heavier particle is introduced on the top of the pond, it must traverse the depth of the pond. It is moved along the bottom of the pond by scrolling action of a conveyor screw operating in the conveyor.
  • a representative disk centrifuge is shown in literature of several manufactures. The heavier particles are forced toward the bottom of the pond with extreme forces applied to the heavier particles during centrifical operation. The centrifical forces are 1000 times greater than the force of gravity, and can even be pushed as high as about 2000 or greater.
  • the particles react to this force by settling to the bottom of the pond and migrating at urging of the screw conveyor to emerge from the disk centrifuge at the beach end of the conveyor. This dumps the heavier particles out of the centrifuge in a significantly dry status. While not dry completely, they from a relatively dry slurry which is significantly free of water. To be sure, some of the water is bound in the solid particles as for example by wetting the cellulose that makes up the food stuff. Pulp and other food related components will typically be removed at this stage.
  • the system 10 delivers components where the gradation between water and starch based food stuffs and heavier pulp can be adjusted.
  • the water can be disposed of as previously noted, the pulp and other components at the heavy end form a slurry of value, and the starchy gelatinous mass has significant value.
  • a CPU 70 is included for operation of one or several valve operators 72. The CPU is used to control the operation of the system.
  • each of the tanks 22 is provided with a level controller 74. These duplicate controllers enable measurement of the volume of the tanks.
  • the flow output is carefully monitored and controlled in both volume and temperature.
  • This can be used to operate the output pumps 26 and 28.
  • Proper operation of the equipment shown in Fig. 1 is enhanced by installing pressure meters 7 6 at respective illustrated locations. In general terms, the pressure meters help the operation because they measure the pressure and indirectly control the flow rates.
  • the pumps 26 and 28 are operated to achieve the set point pressures.
  • the membrane separator 3 2 operates with a selected pressure.
  • the pressure meters 76 are located in the system to assure system control. Likewise, a thermostat 78 is included in the tank 22. This can be duplicated in other locations. All the sensors 74 , 76 and 78 connect to the CPU to assure input of data sufficient to make the necessary measurements and output needed control signals.
  • the outlets of the system 10 shown in Fig. 1 include three outlets. Flows to these outlets are controlled by a number of valves. There are several valves 80 at various locations. In general terms, the valves 80 are opened are closed. It is possible to install and operate valves that are modulated. However, that makes the controller somewhat more complicated. Control is generally implemented by control of the pump speeds. The pumps 26 and 28 are thus operated at appropriate adjustable speeds to obtain the desired pressure ratings at various locations in the system. These pump speeds are carefully selected so that the appropriate pressures downstream are obtained. The valves 8 0 are adjusted to switch different operational aspects. To pick an easy example, the line 18 is the feed line while the line 24 is the feedback line. The line 24 is selectively controlled so that the feedback is delivered either to the tank 20 or the tank 22.
  • Valves are operated so that the feed line 1 8 inputs to the first of the second tank. By appropriate switching of these two, suitable control is obtained. Likewise, the valves are adjusted to enable the return lines around the tanks 20 and 22. This may be necessary to recycle and continuously stir the material in the tanks 20 and 22. In general terms, the valves 80 are simply on/off valves as noted. The valve 82 however is an adjustable valve. It selects the proportion of feed which is input to the disk centrifuge. This assures that the centrifuge is not flooded. When flooding occurs, an excess of liquid is observed in the feedback line 24 . The percent or quantity of solids which are segregated may well suffer from flooding.
  • the system operates with a liquid or clarified water outlet 84 .
  • a concentrate outlet line 86 is likewise provided.
  • the centrifuge 30 has an outlet line for solids which are delivered to the outlet 88 . If desired, the outlet 86 can be closed off so that only solids are delivered through the line 88 and clarified water is delivered through the line 84.
  • Fig. 6 of the drawings shows an embodiment 90 which is quite similar to the system just described except that it includes two centrifuges deployed in series.
  • the system 90 is otherwise similar except that the preliminary centrifuge 92 is a decanter centrifuge.
  • the system incorporates a boiler 94 which provides heat for the several tanks. This assures that the temperatures are raised to the desired level.
  • the outlet stream is tested in all points in time by a viscosity meter 96.
  • Two parallel tanks are included at 22 and 98. By appropriate switching, they can handle flow on a continuous basis or by alternating, thereby operating in a batch basis.
  • the equipment can be located at a central collection point within trucking range of several plants. The plant liquor from several plants can be trucked to that location for treatment, reclamation, and ultimate return of the starch components.
  • Fig. 1 includes the many valves provided with valve operators.
  • the CPU 70 provides control signals to the several valve operators which are connected to the valves. In the particular embodiment shown in Fig. 6, many valves are included which operate in the same fashion.
  • each valve is provided with its own operator.
  • the CPU 70 forms the appropriate set signals for the several valve operators. This enables the system to adjust each valve operator so that the flow through the system is appropriate.
  • Appropriate sensors are located in the system as noted. Typically, the responsive sensors have inputs to the CPU 70.
  • the present disclosure utilizes the membrane which has the form of the folded tube shown in Fig. 4.
  • the U-shaped tube 40 is folded any number of times for directing the waste stream through a series of the tubes. Since the tubes making up the membrane 40 come in a fixed and finite length, the total length is achieved simply by serially connecting the tubes together. As shown in Fig. 3 of the drawings, both input and output to the membrane tubes 40 are at the right hand end. A single pass of the waste stream is achieved on flow to the left and a second pass occurs with return back to the right hand end, just as shown in Fig. 4. If the tube 40 is 40 feet in length (approximately the maximum length suitable for the towed trailer), then the flow path for the tube shown in Fig.
  • N is an even numbered integer and is 2, 4, 6, 8...
  • Fig. 6 of the drawings shows the waste stream flowing through the first and second centrifuges. The last cut is achieved in the membrane system 32. The waste cut, however, from the membrane 32 is improved or enhanced by extending the length of the membrane. Using the above stated formula, if the membrane tube is 480 feet, or perhaps 640 feet, then the amount of solvent pulled from the waste stream is increased and a greater level of purification is obtained. Interestingly, if feedback occurs at that juncture, the length of the membrane tube can be decreased and yet the amount of waste removed by the centrifuges is increased.
  • This feedback line 24 operates in conjunction with the two tanks. The feedback line is directed from the output of the membrane separator 32 to return the feedback to one.
  • This feedback directs the flow out of the membrane separator 32 to the storage tank 22. Consider for the moment that 75% of the material output in the waste stream from the membrane separator is switched back through the feedback line. If that occurs, the gross waste output is actually reduced and the amount of waste output from the elsewhere is increased.
  • the major material which is selectively removed includes starches and the like. These materials are characterized in that they do not easily come out merely by centrifuging; rather, they need to be modified at least somewhat in the membrane separator 32. Basically, the individual, generally unconsolidated starch molecules become more cohesive after passing through the membrane separator 32 and are then more readily removed in the second centrifuge 30.
  • a modified batch operation is set forth. Initially, the description sets forth the centrifuge 30 and the two tanks which provides the flow for the centrifuge 30. By judicious control of the level in each tank, operation can be controlled readily. However, a modified mode of operation is well worth considering. Operation where the flow is directed through the first centrifuge 92, the second 30 and then through the membrane separator 32 will be deemed continuous flow processing. The process is modified by replicating the tank 22 with a second tank 98. With appropriate control valves, one or both of the tanks can be filled to a specified level. Operation of the system on a batch basis then proceeds as follows. Flow is introduced and ultimately delivered into the tank 22.
  • the tank 22 is filled to a specified level and flow is then stopped.
  • the tank 22 is then pumped to deliver flow through the centrifuge 30 , and ultimately .through the membrane separator 32 . It is then delivered out of the membrane separator 32 and directed to the feedback line 24.
  • the feedback returns the concentrate from the membrane separator 32. It is restored back to the tank 22.
  • the tank is then refilled with the feedback flow.
  • Controlled operation of the system whether running in a continuous mode, or operating on a modified batch basis as just described, monitoring of the output stream can be accomplished easily by installing a viscosity meter 96 in the output line 90.
  • the output line delivers the flow of concentrated solids and other materials with a minimum flow of solvent.
  • the viscosity meter 96 is connected to the CPU 70 which in turn operates valve operators 72 to control the valves.
  • the viscosity meter 96 is therefore used to determine the flow output, and is especially significant in observation of the viscosity, thereby reducing the amount of solvent which is wasted in the waste stream through the waste line.
  • the viscosity meter forms a signal input through the CPU so that processing is repeated as necessary to recover more of the solvent, thereby raising the thickness or viscosity of the flow to a desired range.
  • the viscosity measurement triggers operation of the systems so that the starch components are removed typically at the first centrifuge, and somewhat less so at the second centrifuge, and the light weight components which are not so easily removed because of a lack of weight differential are then concentrated i.e. the starch molecules coagulate or agglomerate.
  • the materials removed by virtue of their greater density make up part of the waste stream through the waste line and the large molecules of starch which do not have any weight differential are also removed.
  • the entire output of the membrane separator 3 2 is redirected through the feedback line 24 , and the only waste outlet line is from the centrifuges 30 and 92.
  • the waste from the centrifuge 30 carries those components that are more difficult to separate.
  • FIG. 7 Attention is now directed to the block diagram schematic of Fig. 7 where the entire system is identified by the numeral 1 1 0 where the description will proceed from the input to the output.
  • the description will begin with an assumption that the feed is typical or common to that which is encountered in well drilling situations.
  • the waste stream of interest is the mud stream (other well fluids will be discussed separately) from the drilling rig. It is a stream exemplified by 1 ,000 barrels which constitutes about 25 percent solids by weight in the solvent. Examples of the solvents and the weight materials in the mud stream will be detailed later.
  • the spent drilling mud is delivered in a tank 1 12 .
  • the tank can be a field located mud pit or barge delivery of the drilling mud.
  • the tank 112 is delivered immediately to the equipment 110.
  • the heat exchanger 116 is provided with a flow of hot water or steam from- a boiler 118.
  • the output of the heat exchanger 116 is a flow of the waste stream at a raised or selected temperature. It is delivered to a first centrifuge which is known as a decanting centrifuge.
  • the centifuge 120 has two outputs, one of which is the concentrated flow of waste. In this example, it will remove the heaviest particles in the stream. Representative values of this again are given below.
  • the lighter discharge from the decanting cetrifuge 120 is output to another heat exchanger 122. This heat exchanger again adjusts, to the extent needed, the temperature of the stream which is then delivered to a disk centrifuge 124. That separates another portion of the solids. Examples again will be given below.
  • the lighter solvent discharged from the centrifuge 124 is then delivered to another heat exchanger 126.
  • This heat exchanger operates in conjunction with a buffer tank 128 , in conjunction with a pump 130.
  • the tank 128 adds to or deletes from the direct flow from the centrifuge 1 24 .
  • Working in conjunction with the heat exchanger 126 it delivers the output flow to the membrane separator 1 32 . That makes the final separation and discharges the relatively pure solvent to a storage tank 134.
  • the waste stream of 1 ,000 barrels is comprised of "palm oil" which costs about $300 per barrel. It is used for drilling in tight formations. After use in the formation, it is then delivered in the dirty or polluted state to the system at the tank 1 12.
  • the synthetic oil is first provided with relatively heavy barites and other weight materials to enhance the weight of the mud system. The relative weight is increased significantly by these components which are added intentionally. Typically, they comprise the heavier components having a specific gravity of perhaps 4.0 or greater.
  • the second centrifuge 124 is adjusted to a different setting to accomplish a different segregation. In this particular instance, it is adjusted so that it removes weight components above a particular specific gravity, thereby discharging 32 percent of the weight materials in the stream.
  • the discharge from the second initial stage centrifuge is then input through the membrane separator 132. It removes all the remaining components.
  • the membrane separator will be discussed before the centrifuge separators so that the contrast between the two can be comprehended. More particularly, the membrane separator is located downstream so that it works the separation of the lightest particles of trash and cuttings found in the spent drilling fluid. This kind of separation is relatively challenging. More noting the challenge is given below. Directing attention back to Fig. 2 of the drawings, the separator 3 2 previously discussed is the same as the separator 132 and details regarding Figs. 2, 3, 4, and 5 are incorporated by reference.
  • a representative dual centrifuge system is set forth herein.
  • the dual stage centrifuge system usually is a skid mounted structure. Hence, while heavy on the one hand, it is nevertheless portable because the size readily adapts to a flat bed skid which is moved to the rig site.
  • both the centrifuges and the membrane separator tube assembly mounted on the truck in Fig. 2 are easily moved.
  • all this equipment can be installed at an offshore platform where drilling is conducted around the clock for two or three years to drill a set of wells from a single platform. Equally, the equipment can be moved to a field location where one or more wells are drilled onshore.
  • the equipment can be located at a central collection point within trucking range of several wells and the spent well fluids from the several wells can be trucked to that location for treatment, reclamation, and ultimate return of the segregated solvent and components to the drilling rig or storage.
  • Fig. 7 includes a number of valves 166 which are located at various points. Each valve 166 has a similar construction. The several valves 166 are provided with valve operators. Fig. 1 further includes a CPU 170 which provides control signals to the several valve operators 172.
  • the operators 172 are connected to the valves at 162.
  • many valves are included which operate in the same fashion. While they may differ in the fluid handled and the subpoints applied to the individual valves, they all operate in the same fashion by signals provided to the valve operators 172 .
  • each valve is provided with its own operator.
  • the CPU 1 70 forms the appropriate set signals for the several valve operators. This enables the system to adjust each valve operator so that the flow through the system is appropriate.
  • Appropriate sensors are located in the system.
  • the heat exchangers are provided with temperature responsive sensors 174 which have inputs to the CPU 170.
  • the discharge of the two centrifuges 120 and 124 is output through flow measuring sensors 1 7 4 which again form input signals to the CPU 170 and which is adjusted to thereby control operation of the system. If the flow is inappropriate from either of the centrifuges, the flow rate is then adjusted. This adjustment is carried out by changing the operation of the pump 1 14.
  • the pump 130 is also manipulated to assure the appropriate flow rate into the membrane separator 132.
  • the present disclosure utilizes the membrane which has the form of the folded tube shown in Fig. 4.
  • the U-shaped tube 40 is folded any number of times for directing the waste stream through a series of the tubes. Since the tubes making up the membrane 40 come in a fixed and finite length, the total length is achieved simply by serially connecting the tubes together.
  • FIG. 7 of the drawings shows the waste stream flowing through the first and second centrifuges 120 and 124.
  • the last cut is achieved in the membrane system 132.
  • the waste cut, however, from the membrane 132 is improved or enhanced by extending the length of the membrane.
  • the membrane tube is 480 feet, or perhaps 640 feet, then the amount of solvent pulled from the waste stream is increased and a greater level of purification is obtained.
  • the length of the membrane tube can be decreased and yet the amount of waste removed by the second centrifuge 124 is increased.
  • This feedback path includes the feedback line 180 which operates in conjunction with the two valves 176 and 178.
  • the feedback line is directed from the output of the membrane separator 1 32 to return the feed back to the surge tank 122 .
  • This feedback directs the flow out of the membrane separator 132 to the storage tank 122.
  • the amount which is sent back for recycling depends on the settings of the valves 176 and 178. Consider for the moment that 75% of the material output in the waste stream from the membrane separator is sent back through the feedback line 180. In other words, the valves 176 and 178 are adjusted so that 25% of the output is delivered through the valve 176 which is the output of discarded waste, and the remaining 75% is transferred through the line 180 back into the cleaning cycle. If that occurs, the gross amount of waste output through the valve 176 is actually reduced and the amount of waste output from the centrifuge 124 is increased.
  • the curve in Fig. 8 sets this out.
  • the abscissa relates to the length of the membrane tube. As it is increased, greater length increases the relative portion of the waste that is segregated from the solvent by the membrane tube. With the feedback, however, the modest elongation of the membrane tube cooperates to make the centrifuge 124 more potent, thereby removing more of the waste at that stage, and producing a relatively clarified stream for the membrane separator 132.
  • the feedback cycle will stabilize at appropriate flow rates and waste discharge rates for the second centrifuge and separately for the membrane separator. In general terms, more waste is delivered from the second centrifuge, thereby providing the membrane tube with a larger per cent of solvent to the remaining waste to assure that the flow velocity is maintained within the specified velocity limits.
  • a modified batch operation is set forth.
  • the description set forth the initial input tank 1 16 which provided the flow for the centrifuge 1 20 and the tank 122 which provides the flow for the centrifuge 124.
  • the level in each tank By judicious control of the level in each tank, operation can be controlled readily.
  • a modified mode of operation is well worth considering. Operation where the flow is directed through the first centrifuge, the second and then through the membrane separator will be deemed continuous flow processing.
  • the process can be modified by replicating the tank 122 with a second tank 182. With appropriate control valves, one or both of the tanks can be filled to a specified level. Operation of the system on a batch basis would then proceed ass follows.
  • Flow is introduced through the pump 114 and ultimately delivered into the tank 122.
  • the tank 122 is filled to a specified level and flow is then stopped.
  • the tank 1 22 is then pumped to deliver flow through the centrifuge 124 , and ultimately through the membrane separator 122. It is then all delivered out of the membrane separator 1 32 and directed to the feedback line 180.
  • the feedback returns the concentrate from the membrane separator 132. It is restored back to the tank 122 .
  • the tank 122 is then refilled with the feedback flow.
  • Controlled operation of the system whether running in a continuous mode, or operating on a modified batch basis as just described, monitoring of the output stream can be accomplished easily by installing a viscosity meter 188 in the output line 190.
  • the output line 190 delivers the flow of concentrated solids and other materials with a minimum flow of solvent.
  • the viscosity meter 188 is connected to the CPU 170 which in turn operates valve operators 172 to control the valves.
  • the viscosity meter 188 is therefore used to determine the flow output, and is especially significant in observation of the viscosity, thereby reducing the amount of solvent which is wasted in the waste stream through the waste line 190.
  • the viscosity meter forms - a signal input through the CPU so that processing is repeated as necessary to recover more of the solvent, thereby raising the thickness or viscosity of the flow to a desired range. This is especially beneficial in terms of controlling the two types of separators.
  • the viscosity measurement triggers operation of the systems so that the weight components are removed typically at the first centrifuge 120 , and somewhat less so at the second centrifuge, and the light weight components which are not so easily removed because of a lack of weight differential are then concentrated i.e. the starch molecules coagulate or agglomerate.
  • the materials removed by virtue of their greater density make up part of the waste stream through the waste line 190 and the large molecules of starch which do not have any weight differential are also removed. Moreover, solvent in the stream 190 is reduced.
  • valve 196 can be closed so that the entire output of the membrane separator 132 is redirected through the feedback line 180 , and the only waste outlet line is from the centrifuges 120 and 124 .
  • the waste from the centrifuge 1 2 4 carries those components that are more difficult to separate.
  • Fig. 9 shows a flow delivered to a first centrifuge cooperative with a second separator and then a third separator.
  • these are identified by the reference numerals 202 , 204 , and 206. They make up the major components of the separator system 200 .
  • the flow is introduced into the first centrifuge.
  • the purified and cleaned output is delivered through the line 214.
  • There is an output for waste which is the line 212.
  • the lines 212 and 214 comprise the only output lines in this instance.
  • a feedback loop 210 which includes the branches 216 and 218 as will be described. Suitable valves control the amount of feedback and the delivery or destination of the feedback.
  • centrifuge As the first input device. This is especially the case where heavy ingredients are found in the flowing slurry. This may not always be the situation with certain food processing plants. It is generally, however, true of processing plants dealing with drilling fluids. It is especially effective for taking out the heavy weight materials which run a relative weight of four times greater than the solvent which normally is water or at least a solvent which has a specific gravity approximating water.
  • the device 202 is commonly a centrifuge. The first device therefore is intended to take out the relatively heavy components and deliver them to the waste stream flowing in the line 212 .
  • the second and third separators can be similar or different centrifuges or membrane separators, and the two need not always be arranged with the membrane separator as the third separator. Accordingly, heavy components are taken out first by the first centrifuge and the remaining components including the solvent pass through both the second and third separators.
  • the feedback line is directed from the output of the third separator, meaning the output line 214 , and the feedback line 210 goes back to one of the earlier devices. There are times when it may be more desirable to input the feedback flow into the first centrifuge, but there may be circumstances where it is equally beneficial to input it only to the second separator input. There might be circumstances where splitting the flow between the line 216 and 218 is suggested.
  • the more common approach is to use the first centrifuge to remove the heavy constituents.
  • the second and third separators then operate in a feedback mode so that an adequate amount of the solvent is returned to keep the heavy components in suspension and to continue to obtain the desired velocity through the membrane separator whether it is the second or third separator.
  • This enables certain of the heavy components drop out.
  • the flow continues on so that the desired products are then separated.
  • the heavy components in a drilling fluid situation may be salvaged and recovered having great value while the intermediate or light weight solids coming out of the drilling fluid are not worth recovery as a product. To be sure, they are removed, but they constitute a waste stream.
  • the first centrifuge should then have a discharge, but not to the waste line 212 , but rather to a storage container so that the waste constituents from the second and third separators are then delivered through the waste line 212.
  • the centrifuge 202 is simply discharged without co-mingling with the waste streams from the other separators.
  • the feedback line should be emphasized. It is provided with valves to control a proportion of feedback, and additionally valves are used in the branches 216 and 218 to control the destination of the feedback. That can vary depending on the requirements.

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Abstract

Un système portatif de récupération des boues de forage comprend un réservoir (112) d'admission, un chauffage facultatif destiné à changer la température des boues (118), une première centrifugeuse (122) qui sépare les particules de boue les plus lourdes, une deuxième centrifugeuse (124) qui sépare par ordre les particules de boue lourdes restantes et un étage (132) de filtration final se présentant sous forme d'un tube allongé formé d'un matériau à membrane. Le tube rejette dans les boues les déchets restants qui se présentent sous forme de concentré, et le solvant présent dans l'écoulement de boues traverse la membrane. Le solvant est récupéré pour être ensuite réutilisé et recyclé. Une autre forme de réalisation permet de traiter des liqueurs de plantes alimentaires comprenant de l'amidon, de la pulpe et des produits alimentaires dérivés similaires.
PCT/US1999/013405 1998-06-12 1999-06-14 Systeme de traitement WO1999064356A1 (fr)

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US9729498A 1998-06-12 1998-06-12
US09/097,294 1998-06-12
US09/099,166 1998-06-18
US09/099,166 US5997652A (en) 1998-06-18 1998-06-18 Food starch processing method and apparatus
US09/187,239 1998-11-06
US09/187,239 US6177014B1 (en) 1998-11-06 1998-11-06 Cesium formate drilling fluid recovery process
US09/260,745 US6155964A (en) 1999-03-01 1999-03-01 Centrifuge drive system providing optimum performance
US09/260,745 1999-03-01

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US7935261B2 (en) 2008-11-24 2011-05-03 Arkansas Reclamation Company, Llc Process for treating waste drilling mud
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EP1186645A1 (fr) * 2000-08-03 2002-03-13 Hanseland B.V. Fluides de forage comprenant de l'amidon à teneur élevée en amylose
WO2003033541A1 (fr) * 2001-10-15 2003-04-24 A.E. Staley Manufacturing Co. Filtration sur membrane permettant l'epaississement et le lessivage d'amidon dans l'extraction de l'amidon du mais par voie humide
US6648978B2 (en) 2001-10-15 2003-11-18 A. E. Staley Manufacturing Co. Membrane filtration for thickening and starch washing in corn wet milling
US7867399B2 (en) 2008-11-24 2011-01-11 Arkansas Reclamation Company, Llc Method for treating waste drilling mud
US7935261B2 (en) 2008-11-24 2011-05-03 Arkansas Reclamation Company, Llc Process for treating waste drilling mud
WO2011112831A2 (fr) 2010-03-10 2011-09-15 M-I L.L.C. Système et procédé pour séparer des matières solides d'un fluide
EP2544799A4 (fr) * 2010-03-10 2016-11-16 Mi Llc Système et procédé pour séparer des matières solides d'un fluide
EP2545244A4 (fr) * 2010-03-10 2016-11-16 Mi Llc Système et procédé pour séparer des matières solides d'un fluide
US10029213B2 (en) 2010-03-10 2018-07-24 M-I L.L.C. System and method for separating solids from fluids

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WO1999064356A9 (fr) 2000-03-09

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