CA1116536A - Process for removal of suspended solids from liquid - Google Patents
Process for removal of suspended solids from liquidInfo
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- CA1116536A CA1116536A CA000326251A CA326251A CA1116536A CA 1116536 A CA1116536 A CA 1116536A CA 000326251 A CA000326251 A CA 000326251A CA 326251 A CA326251 A CA 326251A CA 1116536 A CA1116536 A CA 1116536A
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Abstract
PROCESS FOR REMOVAL OF
SUSPENDED SOLIDS FROM LIQUID
Abstract of the Disclosure A process for removal of solids from a liquid containing suspended solids by flowing the liquid through a filter bed of discontinuous polyurethane particles in a filtration vessel. For renewal of the filter bed, de-posited solids are removed from the discontinuous poly-urethane particles by adding at least one bed volume of a regeneration liquid to the filter vessel and mechanically mixing the filter bed of polyurethane particles in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from the termination of liquid flow therethrough, thereby forming solids-enriched liquid, and discharging the solids-enriched liquid from the filtration vessel.
S P E C I F I C A T I O N
SUSPENDED SOLIDS FROM LIQUID
Abstract of the Disclosure A process for removal of solids from a liquid containing suspended solids by flowing the liquid through a filter bed of discontinuous polyurethane particles in a filtration vessel. For renewal of the filter bed, de-posited solids are removed from the discontinuous poly-urethane particles by adding at least one bed volume of a regeneration liquid to the filter vessel and mechanically mixing the filter bed of polyurethane particles in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from the termination of liquid flow therethrough, thereby forming solids-enriched liquid, and discharging the solids-enriched liquid from the filtration vessel.
S P E C I F I C A T I O N
Description
3~
~ACKGROUND OF THE I~ENTTON
Field of the Inventlon This invention relates to a process for removal of solids from a liquid containing suspended solids by flowing the liquid through a filter bed of discontinuous polyurethane particles.
Descr~tion of the Prior Art In the field of liquid and wastewater treatment, filtration has long been a major method of removing sus-pénded solids from liquid streams. In wastewater treat-ment applications in particular, the presence of suspended solid materials is frequently a major process problem and filtration has commonly been employed as a means of reducing and/or removing suspended solids from st~eams such as municipal sewage and wastewater intended for re-cycle use. In such applications, clownflow and upflow sand filters and dual or mixed medla filters ha~e been widely ernployed and have in general been shown to be cost effective and efficient in use. Nonetheless, work by practitioners in the field has shown that sand and mixed media filters are in general effective in removing suspended solids, but only under limited solids loading conditi~ns. In general, solids concentration of the liquid stream entering the filter must be below about 100-200 milligrams/liter. ~ ~ ~
6.153~
At suspended solids concentration values above this level, the filtration bed is susceptible to clogging and high pressure drop across the bed.
In recent years, the operatlon of filtration has been somewhat improved in the foregoing applications by the use of polyurethane as a filtration medium. In general practice, polyurethane foam is cut up into _mall pieces and placed into a retaining vessel to form the filtration bed. Wastewater or other liquid containing suspended solids is then flowed through the bed ~ith re sulting deposition of suspended solids on the polyurethane particles. The suspended solids thus remain on the poly-urethane particles and the liquid from which the sus-pended solids has been deposited subsequently passes through the bed and is discharged as liquid depleted in suspended solid contaminants.
In general, the use of polyurethane foam as a flltration medium provides numerous operating advantages over beds employing sand or conventional mixed media filtration materials, including higher solids capacity, lower pressure drop head losses, higher resistance to clogging and removal of numerous soluble organic contam-inants from the liquid stream.
Despite its numerous operating advantages, however, regeneration of the polyurethane foam which has become loaded wlth suspended solids in the filtration operation has continued to pose a severe operating problem.
Various methods have been contemplated for regeneration of the polyurethane ~oam filtration bed which has become 3o ~t least partially loaded with suspended solids during the lV~ JUL
31~
flltration step, including back-washing with a solids-depleted liquid stream, such as is commonly employed in conventional sand and mixed media filtration systems.
The use of back washing in a polyurethane foam filtration bed poses a specific problem due to the low density of the polyurethane foam filtration medium. Since poly-urethane has a true density which may be as low as 1 - 2 pound/foot , it ls generally desirable in normal operation to flow liquid containing suspended solids do~mwardly through the bed of polyurethane foam material. Back washing of such a filtration bed, which involves counter-currently flowing a stream of clean liquid upwardly through the filtration bed, in general requires such ~gh flow velocities through the bed as to wash particles of poly-urethane foam out of the bed or else causessuch disruption of the bed as to leave large void spaces therein which contribute to bypassing and other disadvantageous per-~ormance behavior in the subsequent filtration step. If, on the other hand, the bed of polyure-thane foam is re-generated in the same manner as the normal filtration step, by flowing a stream of solids-depleted liquid downwardly through the solids-loaded bed, it is generally difficult to obtain sufficient removal of suspended solids from the polyurethane particles to satisfactorily renew the bed for the subsequent filtration step.
~aced wlth the foregoing difficulties in the application of conventional back washing to the polyure-- thane foam filtration bed, and in view of ~he extremely low density of the polyurethane foam f~ltration medium re~ative to conventional media, the prior art has proposed ~ 3~D
varlous means for compression regeneration of the polyure-thane foam ln the filtration bed. Such compression re-generation generally involves the use of mechanical means for "squeezing" the particles of polyurethane foam, there-by "wringing out" the contained water along with the deposited solids from the particles of polyurethane foam.
Although such method of regeneration is easily employed on a laboratory or bench-scale filtration unit, the mechanical complexity and attendant capital expense of means for squeezing the foam particles in commercial scale polyure-thane foam filtration beds has severely limited the utility of polyurethane foam f~ltration beds in practice.
Accordingly, it is an object of the present -in-vention to provide an improved process for removing de-posited suspendéd solids from polyurethane partiCles in a filtration bed of such particles.
It is another object of the invention to provide such a process which requires only a very low volume of regeneration liquid.
Other objects and advantages of the present invention will be apparent from the ensuing disclosure and appended claims.
SUMMARY OF THE INVENTION
This invention relates to a p~ocess for removal - of sollds from a liquid containing suspended solids.
Tn t~e process of this invent~ on, a filtration vessel containing a filter bed of discontinuous polyure-thane particles is provided. The liquid containing sus-pended solids is flowed through the filter bed in the 10~61 filtration vessel for deposition of the solids on the polyurethane particles to form solids-depleted liquid and sollds-depleted liquld is discharged from the filtra-tion vessel, until the filter bed is at least partially loaded with removed solids. The flow of liquid through the filter bed is terminated. Deposited solids are re-moved from the discontinuous polyurethane particles in the filter bed, thereby renewing the filter bed for solids removal from the liqu~d containing suspended solids.
In the improvement of the invention, the re-moval of deposited solids from the discontinuous polyure-thane particles in the filter bed is carried out by adding at least one bed volume of regeneration liquid to the filtration vessel and mechanically mixing the filter bed of discontinuous polyurethane particles having the solids deposited thereon in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from the termination of liquid flo~
through the ~ilter bed to cause deposited solids to dis-engage from the discontinuous polyurethane particles and pass into the total volume of liquid, thereby forming solids-enriched liquid. The solids-enriched liquid is discharged from the filtration vessel.
In one preferred embodiment of the present invention the filter bed occupies no more than one-half the volume of the filtration vessel, and the mechanical mixing comprises mechanically agitating the filter bed of polyurethane particles.
In another preferred embodiment of the present invention, the regeneration liquid comprises between one and two bed volumes of liquid.
As used herein, "regeneration liquid" means liquid which is able ~o take up in suspended form the deposited solids which are disengaged from the filter bed of poly-urethane particles during the mechanical mixing thereof. In preferred practice, the regeneration liquid is substantially free of suspended solids. As use~ herein, "hold-up liquid in the filter bed" refers to the interstitial liquid be-tween particles of polyurethane and to the liquid which is retained in the pores of the polyurethane particles in the filter bed subseque~t to termination of liquid flow through the filter bed. "Bed volume" means a unit volume of liquid which is equal to the volume of the filter bed BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic diagram of a filter bed of diseontinuous polyurethane par~icles, such as may suit-ably be used in the practice of the present invention.
.
Figure 2 is a schematic view of the Figure 1 filter bed during the regeneration step.
Figure 3 is a schematic diagram of another embodiment of the present invention, wherein a filter bed of discontinuous polyurethane particles is disposed upstream of a conventional sand filter.
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BRIEF DESCRIPTION OF THE PREFERRED EMBODI~ENTS
Referring now to Figure 1, liquid containing suspended solids enters the treatment system in line 100 having control valve 115 disposed therein, which is open during the initial phase of operation. This liquid may be from a variety of sources9 as for example a biological treatment plant effluent having 40 - 60 parts per million suspended solids or river water for a municipal water treat-ment facility. Alternatively, the liquid could comprise raw water intended for boilers or for internal industrial plant use or it could be a stream from an algae pond (oxidation ditch) which is treated to prevent pin-point algae flocs from reaching the receiving wa~ers. Fr~m line 100, the liquid enters the filtration vessel 102 and is dis-charged in the upper end thereof through a spray distributor or other discharge device 101. The filtration vessel 102 may suitably be constructed from carbon steel or other structural material and is only partially filled with a filter bed of discontinuous polyurethane particles 103, for reasons which will be more fully apparent hereinafter. The filtration vessel has an upper inlet end and a lower dis-c~arge end. The filter bed of discontinuous polyurethane particles is supported within the vessel by a lower support-ing structure 104, which may suitably comprise a retaining grid of screen or other fine mesh material. In ~his manner ~ 3`~
a plenum space 10.5 is formed at the lower end of the vessel 102, for collection of the liquid which has been passed through the filter bed.
The liquid containing suspended solids is flowed through the filter bed in the filtration vessel from the upper inlet end to the lower discharge end for deposition of the solids from the liquid on the polyurethane particles, to effect removal of the solids by the filter bed. Solids-depleted liquid is thereby formed which collects ;n the lower plenum space 105 and is discharged from the filtration vessel in line 106, having open control valve 116 disposed therein. From line 106, the solids-depleted liquid is passed to receiving waters and/or other treatment and end use.
The previously described flow of liquid containing suspended solids is continued until the filter bed is at least partially loaded with deposited solids, whereupon the flow of liquid through the filter bed is terminated, and the filter bed is ready for renewalO
In order to enhance the solids collection re-moval efficiency of the filter bed in the previously des-cribed system, it may be desirable in some instances to add a coaugulant ma~erial, such as an organic polymer coa~ulant, sodium silicate or alum, to the liquid being introduced to the filter. Such coaugulants are in some applications desirable in order to increase the flocculation of suspend-ed solids in the liquid undergoing treatment and to reduce ~he turbidity of ~he final effluent discharged from the filter bed treatment sys~em.
The polyurethane particles employed in the filter bed of the present invention may be of any suitable foam type having the requisite solids loading capacity for the filtration step operating time employed. The discontinuous polyurethane employed in the particles of the fil~er bed may suitably be in the form of shredded non-uniformly sized particles or, alternatively, ~he polyurethane particles in the filter bed may have a cubic form, as may be obtained by physically cutting a body of polyurethane foam into small sized particles such as cubes having sides of 1/4 to 1 inch length. Suitable polyure~hane foam materials which have been employed successfully in practice have a cellular density of from 10 ~o 100 cells/inch. The true density of the poly-urethane particles in the filter bed should preferably be greater than about 1.34 lbs./ft. in order to provide structural integrity of the bed and to preclude floating of the polyurethane particles during the filtration step The polyurethane particles in the filter bed preferably have a solids loading capacity of at least one-half pound suspend-ed solids/ft polyurethane particles, in order to provide suitably high capacity for solids loading during the filtra-tion step. By way of example, a suitable foam polyurethane ;53~ 1 material for use in the process of the present invention may be shredded in form, with particle lengths on the order of 1 - 2 inches, 30 cells/linear inch, a particle thickness on the order of 0,25 inch, a true density (measur-ed without voids) of 1.77 lbs./ft. and a tensile strength of 23 5 psi.
During the filtration step, the volumetric flow velocity of the liquid containing suspended solids through the filter bed is desirably maintained between 1 and 10 gal/minute/ft of filter bed cross-sectional area, in order to provide adequate contacting of the liquid with the polyurethane particles i~ the filter bed without the occurr-ence of bypassing or other anomalous flow phenomens. After the filter bed is at least partially loaded with deposited solids, the flow of liquid through the filter bed is termin-ated. Subsequently, deposîted solids are removed from the discontinuous polyurethane particles in the filter bed, thereby renewing the filter bed for solids removal from the liquid containing suspended ~
,,-.. _ _ _ _ _ .. .... . . , .. . , . .. . . ...... _ _ _ ........ .
lU~l Prior to the renewal step, the flow of liquid through the filter bed 103 is terminated, as for example by closing the control valves 115 and 116 in lines 100 and 106 re-spectively. At the termination of flow of liquid through the filter bed, hold-up liquid will remain in the filter 103. In the renewal step, at least one bed volume of a regenera~ion liquid is added to the filtration vessel 102, to form a total volume of liquid in the filtration vessel comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from ~he termination of liquid flow through the filter bed. Figure 2 shows the sys~em of Figure 1 wherein the filtration vessel contains the afore-mentioned total volume of liquid. Prior to the addition of regeneration liquid to the filtration vessel, the filtration vessel will generally contain sufficient hold-up liquid to constitute a major fraction of a bed volume of liquid due ~o the high porosity of the fil~r bed of poly-urethane particles. For example, the porosity of the filter bed of polyurethane particles may be on the order of 80%, whereby the filtration vessel at the termination of liquid flow through the filter bed would contain 0.80 bed volume of hold-up liquid as interstitial liquid between the part-icles of polyurethane and liquid retained in the pores of the polyurethane particles in the filter bed.
As stat~d earlier herein, the term "bed volume"
means a unit volume of liquid which is equal to the volume . - 12 ~ 3~
of the f~lter ~ed Thus, if a fil~er bed is provided which ls two feet ln height in the filtration vessel, the addition of one bed volume of additional liquid (regeneration liquid) would resul~ in the provision of an admixture of polyurethane particles and liquid phase wherein the height of the liquid in the filtration vessel would be 4 ft.
The regeneration liquid added to the filtration vessel in the renewal step may comprise liquid containing suspended solids which is introduced to the filtration vessel in line 100, following which valve 115 in line 100 is closed. Alternatively, the regeneration liquid may comprise solids-depleted liquid, as for example clean water, when the liquid containing suspended solids is water.
The solids-depleted liquid may be introduced countercurrent-ly into the filtration vessel following termination of liquid flow through the filter bed by flow of the regenera-tion liquid through line 113 and countercurrently through that portion of line 106 which is directly benéath filtra-tion vessel 102. In the latter case, valve 114 in line 113 is open, while valves 115 in line 100 and valve 116 in line 106 are closed. During the normal filtration step, valve 114 is closed, while valves 115 and 116 are open.
The switching of the various respective valves may be carried out by a cycle time control system of a type well known to those ~killed in the art.
~ 6 After at least one bed volume of regeneration liquid has been added to the filtration vessel, as shown in Figure 2, all valves 114, 115 and 116 are closed. In preferred practice, the filter bed, as shown in Figure 1, occupies no more than one-half the volume of the fil~ration vessel, so as to allow for introduction of at least one bed volume of regeneration liquid to the filtration vessel. In the regeneratlon step, as mentioned, the filtration vessel contains a total volume of liquid comprising the regenera-tion liquid and the hold-up liquid in ~he filter bed re-sulting from the termination of liquid flow through the filter bed. In the general practice of the present in-vention, the hold-up liquid in the filter subsequent to the termination of liquid flow through the filter bed is intended to be construed broadly so as to include hold-up liquid in the filter bed, constituted by solids-depleted liquid remaining in the bed following the termination of liquid flow therethrough as well as to include the inter-stitial liquid between particles of polyurethane and the liquid which is re~ained in the pores of the polyurethane particles in the filter bed when the filter vessel is drain-ed of liquid following the termination of liquid flow through the filter bed and the hold-up liquid is replaced by a fractional bed volume of regeneration liquid. In other words, it is contemplated in the broad practice of ~he ~ 3~
present invention to completely drain $he filtration vessel of liquid following the filtration step and then to fill the fil~ration vessel with regeneration liquid to the desired extent such that a portion of the total volume of liquid replaces the hold-up liquid which was previously contained between the particles of polyurethane and in the pores of the polyurethane particles in the filter bed.
In this manner, the fractional bed volume of regeneration liquid which fills the pores and interstices of the filter bed becomes the hold-up liquid in the filter bed. Nonethe-less, it is generally preferred in practice to retain the hold-up liquid in the filter bed resulting from the termin-ation o liquid flow through the filter bed in order to min-imize the filter bed regeneration time and to simpl~fy the regeneration procedure.
In the system as shown in Figure 2, after the regeneration liquid had been introduced to the filtration vessel to form a total volume of liquid comprising the re-generation liquid and the hold-up liquid therein, the filter bed of discontinuous polyurethane particles having the solids deposited thereon is mechanically mixed to cause deposited solids to disengage from the discontinuous poly-urethane particles and pass into the ~otal liquid volume, thereby forming solids-enriched liquid. This is carried out by energizing the motor drive means 117 which is 1 ~ O ~ 1 ~ 53~
connected by rotating shaft member 118 to rotating impeller means 119. In this manner, the filter ~ed is mechanically mixed by agitating the polyurethane particles in the total liquid volume in the filtration vessel. Such agitation causes disengagement of the deposited solids from the poly-urethane particles in the bed and forms the aforemen~ioned solids-enriched liquid in the filtration vessel. After a suitable period of agitation, which for example may be 1 - 3 minutes,when disengagement of deposited solids from the polyurethane particles has been effected, the motor drive means 117 is deenergized and the solids-enriched liquid is discharged from the filtration vessel in line 106 by opening of valve 116; The solids-enriched liquid in line 106 may be passed to further treatment and/or end use facilities, such as sludge drying beds. After the solids-enriched liquid is fully discharged from the filtration vessel, the filter bed is fully renewed for the subsequent filtration s~ep, which may be initiated by opening valve 115 in feed liquid line 100 to admit liquid containing sus-pended solids to the filtration vessel 102 for filtration therein as earlier described.
It was stated earlier herein that the regenera-tion liquid preferably comprises between one and two bed volumes of liquid. Such volumetric amounts of regenera-tion liquid are satisEactory in the broad practice of the ~ 3~
present invention to fully regenerate the polyurethane particle filter bed. By way of example, experience has shown that a 30 cell per linear inch polyurethane foam filter bed can be satisfactorily regenerated in one bed volume of regeneration liquid (in addition to the hold-up liquid in the filtration vessel.) A 60 cell per linear inch polyurethane foam filter bed, on the other hand, has been found to require 1.6 bed volumes of regeneration liquid (in addition to the hold-up liquid in the filtra-tion vessel) for efficient regeneration. This difference is due to the fact that the 60 cell polyurethane foam is less dense than the 30 cell polyurethane foam and thus the former requires a correspondingly greater volume for mechan-ical mixing in the regeneration step.
Referring now to Figure 3, ~here is shown a schematic diagram of another process system in which the process of the instant invention can be carried out. Liquid containing suspended solids is introduced into the system in line 200 having con~rol valve 215 disposed therein from which it is distributed by the distributor means 201 a~ the upper end of the filtration vessel 202 to the filter bed 203 of discontinuous polyurethane particles contained in the filtration vessel. The filter bed of discontinuous poly-urethane particles has an u~per inlet end and a lower dis-charge end, with the latter resting on support structure 204~ which provides a lower plenum space 205 for collec~ion ~ 53~
of purified llquid from the filter bed. The liquid contain ing suspended solids is flowed through the filter bed in the filtration vessel for deposi~ion of the solids on the polyurethane particles to form solids-depleted liquid. The solids-depleted liquid is discharged from the filtration vessel 202 in line 206. During the normal filtration step valve 215 in line 200 is open and valve 209 in line 208 is closed.
From line 206, solids-depleted liquid is passed to the downstream filter bed 237 for final effluent polish-ing of the liquid. The do~lstream filter bed 237 may be a conventional sand filter or of a mixed media type. The downstream bed 237 is contained in vessel 236 and receives liquid from line 206 through distributor means 23~, which may be of a type similar to that employed in filtration vessel 202. The liquid flowing through the downstream filter bed 237 is discharged therefrom in line 238 and passed to reeeiving waters and/or other desired end use.
The above-described filtration step is continued until the filter bed is at least partially loaded with deposited solids, at which point the flow of liquid through the filter bed is terminated. The filter bed of polyurethane particles is now ready for renewal by removal of deposited solids from the discontinuous polyurethane particles of the bed, thereby re-establishing the capability of the filter bed for solids removal from the liquid cont~ining suspended ~ 3 solids.
In the renewal step, at least one bed volume of regeneration liquid is added to the filtration vessel 202. The filter bed of discontinuous polyurethane particles having the solids deposited thereon is then mechanically mixed by agitation by energizing motor drive means 217 which is connected by shaft member 218 to impeller means 219. Mixing agitation is carried out for a suitable time, as for example 1 - 3 minutes, in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from termination oE liquid through the filter bed~ to cause deposited solids to dis-engage rom the discontin~ous polyurethane particles and pass into the total liquid volume, ~hereby forming solids-enriched liquid. At this point valve 209 in line 208 is opened and the solids-enriched liquid is discharge~ from ; the filtration vessel in line 208. Subsequent to the dis-charge of solids-enriched liquid from the filtration vessel 202, the filter bed 203 in the vessel is renewed and ready for the normal fil~ration step. The second filter bed 237 may be regenerated in any suitable manner such as by con-ventional back-washing.
The advantages of the present invention are illustrated in the ollowing example.
- 19 ~
~ S3 EXAMPLE
A comparative performance evaluation was carried out on filter beds regenerated by back-washing and by agitation mixing in manner of the present invention. In the evaluation, two filter beds were arranged in parallel flow relationship and were arranged to filter identical respective portions of a common flow of solids-containing waste water. Each bed was contained in a glass column having an inner diameter of 14 centimeters. Each con~ained 75 grams of a 60 cell per linear inch shredded polyurethane foam of approximately 95% porosity which formed filter beds in the respective columns each 23 centimeters in height, at a packing density of 30 grams of polyurethane foam per liter of filter bed volume.
The respective filter beds each processed a flow of 200 milliliters of suspended solids containing waste water per minute. Four separate runs were made with re-generation between successive filtration steps and the fourth run was considered as representative of steady state operating conditions. Each filtration step was carried out for 8 hours. Subsequent to the termination of the filtration step, one of the filter beds was re-generated by back-washing and the other was regenerated by agitation mixing in the manner of the present invention.
In the back-washi~g regeneration step for the ~ 3~
first fil~er bed, clean water was flowed as the back-wash medium through the filter bed in a direction counter-current to the down flow direction of liquid flow through the filter bed during the normal filtration step. In the back-washing step, the back-washing flow rate was 18 gallons per minute per ft. of filter bed cross-sectional area. Re-generation was carried out for 5 minutes, at which ~ime the effluent back-wash liquid appeared to be relatively solids-iree .
In the filter bed regenerated in accordance with the method of the present invention, one bed volume of regeneration liquid ~clean water) was added to the filtra-tion vessel and the filter bed was mechanically mixed in a total volume of liquid comprising the one additional bed volume of regeneration liquid and the hold-up liquid in the filter bed resulting from the termination o~ liquid flow through the filter bed. Following the addition of the re-generation liquid, the filter bed was mixed for two minutes by an impeller comprising four 45 pitched blades. The diameter of ~he mixing impeller was approximately 5 centi-meters and the impeller was rotated dur;ng the mixing agita~
tion s~ep at a rotstional speed on the order 100 - 200 rpm.
The mixing agitation was then terminated and the bed was drained of liquid. The filter bed was then refilled wi~h two additional bed volumes of clean water and again mechan-ically mixed for two minutes. The mixing agitation was again terminated and the bed returned to the filtration operation.
~ 6 Comparative performance data for the respective regener~ion modes are set forth below in Table I.
_ Table I _ _ _ _ _ Comparative Performance of Filter Beds Regenerated by Back-washing and by Agitation Mixin~
Parameter ~ D~tion Method Backwashing Agitation Mixing . . _ ,_ Total Regeneration Liquid Volume, gal. 14 4.5 Solids initially on filter bed PmS 18 18 _ , _ Solids on filter bed after regeneration, ~ms 5 0O5 .~ . _ _ _ Solids re~oved, % 72% 97.5~O
As shown by the data, the backwashing regeneration method required 14 gals. of total regenerativn liquid, whereas the agitation mixing regeneration method of this invention re-quired only 4.5 gals. (note: the total regeneration liquid volume listed in the Table for the agitation mixing method comprises the added bed volumes of regeneration liquid and the hold-up liquid in the filter bed contained in ~he pores and interstices of the filter bed~. As also shown by the - data, the back-washing regeneration method yielded only a 72% solids removal from the filter bed, despite the large volume of regeneration liquid employed, while the agitation mixing regeneration method of the present invention resulted in a 97.5/0 solids removal.
Although preferred embodiment of the invention have been described in detail, it is to be recognized that other embodiments only with modification of the disclosed features are contemplated as being within the scope of the invention.
~ACKGROUND OF THE I~ENTTON
Field of the Inventlon This invention relates to a process for removal of solids from a liquid containing suspended solids by flowing the liquid through a filter bed of discontinuous polyurethane particles.
Descr~tion of the Prior Art In the field of liquid and wastewater treatment, filtration has long been a major method of removing sus-pénded solids from liquid streams. In wastewater treat-ment applications in particular, the presence of suspended solid materials is frequently a major process problem and filtration has commonly been employed as a means of reducing and/or removing suspended solids from st~eams such as municipal sewage and wastewater intended for re-cycle use. In such applications, clownflow and upflow sand filters and dual or mixed medla filters ha~e been widely ernployed and have in general been shown to be cost effective and efficient in use. Nonetheless, work by practitioners in the field has shown that sand and mixed media filters are in general effective in removing suspended solids, but only under limited solids loading conditi~ns. In general, solids concentration of the liquid stream entering the filter must be below about 100-200 milligrams/liter. ~ ~ ~
6.153~
At suspended solids concentration values above this level, the filtration bed is susceptible to clogging and high pressure drop across the bed.
In recent years, the operatlon of filtration has been somewhat improved in the foregoing applications by the use of polyurethane as a filtration medium. In general practice, polyurethane foam is cut up into _mall pieces and placed into a retaining vessel to form the filtration bed. Wastewater or other liquid containing suspended solids is then flowed through the bed ~ith re sulting deposition of suspended solids on the polyurethane particles. The suspended solids thus remain on the poly-urethane particles and the liquid from which the sus-pended solids has been deposited subsequently passes through the bed and is discharged as liquid depleted in suspended solid contaminants.
In general, the use of polyurethane foam as a flltration medium provides numerous operating advantages over beds employing sand or conventional mixed media filtration materials, including higher solids capacity, lower pressure drop head losses, higher resistance to clogging and removal of numerous soluble organic contam-inants from the liquid stream.
Despite its numerous operating advantages, however, regeneration of the polyurethane foam which has become loaded wlth suspended solids in the filtration operation has continued to pose a severe operating problem.
Various methods have been contemplated for regeneration of the polyurethane ~oam filtration bed which has become 3o ~t least partially loaded with suspended solids during the lV~ JUL
31~
flltration step, including back-washing with a solids-depleted liquid stream, such as is commonly employed in conventional sand and mixed media filtration systems.
The use of back washing in a polyurethane foam filtration bed poses a specific problem due to the low density of the polyurethane foam filtration medium. Since poly-urethane has a true density which may be as low as 1 - 2 pound/foot , it ls generally desirable in normal operation to flow liquid containing suspended solids do~mwardly through the bed of polyurethane foam material. Back washing of such a filtration bed, which involves counter-currently flowing a stream of clean liquid upwardly through the filtration bed, in general requires such ~gh flow velocities through the bed as to wash particles of poly-urethane foam out of the bed or else causessuch disruption of the bed as to leave large void spaces therein which contribute to bypassing and other disadvantageous per-~ormance behavior in the subsequent filtration step. If, on the other hand, the bed of polyure-thane foam is re-generated in the same manner as the normal filtration step, by flowing a stream of solids-depleted liquid downwardly through the solids-loaded bed, it is generally difficult to obtain sufficient removal of suspended solids from the polyurethane particles to satisfactorily renew the bed for the subsequent filtration step.
~aced wlth the foregoing difficulties in the application of conventional back washing to the polyure-- thane foam filtration bed, and in view of ~he extremely low density of the polyurethane foam f~ltration medium re~ative to conventional media, the prior art has proposed ~ 3~D
varlous means for compression regeneration of the polyure-thane foam ln the filtration bed. Such compression re-generation generally involves the use of mechanical means for "squeezing" the particles of polyurethane foam, there-by "wringing out" the contained water along with the deposited solids from the particles of polyurethane foam.
Although such method of regeneration is easily employed on a laboratory or bench-scale filtration unit, the mechanical complexity and attendant capital expense of means for squeezing the foam particles in commercial scale polyure-thane foam filtration beds has severely limited the utility of polyurethane foam f~ltration beds in practice.
Accordingly, it is an object of the present -in-vention to provide an improved process for removing de-posited suspendéd solids from polyurethane partiCles in a filtration bed of such particles.
It is another object of the invention to provide such a process which requires only a very low volume of regeneration liquid.
Other objects and advantages of the present invention will be apparent from the ensuing disclosure and appended claims.
SUMMARY OF THE INVENTION
This invention relates to a p~ocess for removal - of sollds from a liquid containing suspended solids.
Tn t~e process of this invent~ on, a filtration vessel containing a filter bed of discontinuous polyure-thane particles is provided. The liquid containing sus-pended solids is flowed through the filter bed in the 10~61 filtration vessel for deposition of the solids on the polyurethane particles to form solids-depleted liquid and sollds-depleted liquld is discharged from the filtra-tion vessel, until the filter bed is at least partially loaded with removed solids. The flow of liquid through the filter bed is terminated. Deposited solids are re-moved from the discontinuous polyurethane particles in the filter bed, thereby renewing the filter bed for solids removal from the liqu~d containing suspended solids.
In the improvement of the invention, the re-moval of deposited solids from the discontinuous polyure-thane particles in the filter bed is carried out by adding at least one bed volume of regeneration liquid to the filtration vessel and mechanically mixing the filter bed of discontinuous polyurethane particles having the solids deposited thereon in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from the termination of liquid flo~
through the ~ilter bed to cause deposited solids to dis-engage from the discontinuous polyurethane particles and pass into the total volume of liquid, thereby forming solids-enriched liquid. The solids-enriched liquid is discharged from the filtration vessel.
In one preferred embodiment of the present invention the filter bed occupies no more than one-half the volume of the filtration vessel, and the mechanical mixing comprises mechanically agitating the filter bed of polyurethane particles.
In another preferred embodiment of the present invention, the regeneration liquid comprises between one and two bed volumes of liquid.
As used herein, "regeneration liquid" means liquid which is able ~o take up in suspended form the deposited solids which are disengaged from the filter bed of poly-urethane particles during the mechanical mixing thereof. In preferred practice, the regeneration liquid is substantially free of suspended solids. As use~ herein, "hold-up liquid in the filter bed" refers to the interstitial liquid be-tween particles of polyurethane and to the liquid which is retained in the pores of the polyurethane particles in the filter bed subseque~t to termination of liquid flow through the filter bed. "Bed volume" means a unit volume of liquid which is equal to the volume of the filter bed BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic diagram of a filter bed of diseontinuous polyurethane par~icles, such as may suit-ably be used in the practice of the present invention.
.
Figure 2 is a schematic view of the Figure 1 filter bed during the regeneration step.
Figure 3 is a schematic diagram of another embodiment of the present invention, wherein a filter bed of discontinuous polyurethane particles is disposed upstream of a conventional sand filter.
i31~
BRIEF DESCRIPTION OF THE PREFERRED EMBODI~ENTS
Referring now to Figure 1, liquid containing suspended solids enters the treatment system in line 100 having control valve 115 disposed therein, which is open during the initial phase of operation. This liquid may be from a variety of sources9 as for example a biological treatment plant effluent having 40 - 60 parts per million suspended solids or river water for a municipal water treat-ment facility. Alternatively, the liquid could comprise raw water intended for boilers or for internal industrial plant use or it could be a stream from an algae pond (oxidation ditch) which is treated to prevent pin-point algae flocs from reaching the receiving wa~ers. Fr~m line 100, the liquid enters the filtration vessel 102 and is dis-charged in the upper end thereof through a spray distributor or other discharge device 101. The filtration vessel 102 may suitably be constructed from carbon steel or other structural material and is only partially filled with a filter bed of discontinuous polyurethane particles 103, for reasons which will be more fully apparent hereinafter. The filtration vessel has an upper inlet end and a lower dis-c~arge end. The filter bed of discontinuous polyurethane particles is supported within the vessel by a lower support-ing structure 104, which may suitably comprise a retaining grid of screen or other fine mesh material. In ~his manner ~ 3`~
a plenum space 10.5 is formed at the lower end of the vessel 102, for collection of the liquid which has been passed through the filter bed.
The liquid containing suspended solids is flowed through the filter bed in the filtration vessel from the upper inlet end to the lower discharge end for deposition of the solids from the liquid on the polyurethane particles, to effect removal of the solids by the filter bed. Solids-depleted liquid is thereby formed which collects ;n the lower plenum space 105 and is discharged from the filtration vessel in line 106, having open control valve 116 disposed therein. From line 106, the solids-depleted liquid is passed to receiving waters and/or other treatment and end use.
The previously described flow of liquid containing suspended solids is continued until the filter bed is at least partially loaded with deposited solids, whereupon the flow of liquid through the filter bed is terminated, and the filter bed is ready for renewalO
In order to enhance the solids collection re-moval efficiency of the filter bed in the previously des-cribed system, it may be desirable in some instances to add a coaugulant ma~erial, such as an organic polymer coa~ulant, sodium silicate or alum, to the liquid being introduced to the filter. Such coaugulants are in some applications desirable in order to increase the flocculation of suspend-ed solids in the liquid undergoing treatment and to reduce ~he turbidity of ~he final effluent discharged from the filter bed treatment sys~em.
The polyurethane particles employed in the filter bed of the present invention may be of any suitable foam type having the requisite solids loading capacity for the filtration step operating time employed. The discontinuous polyurethane employed in the particles of the fil~er bed may suitably be in the form of shredded non-uniformly sized particles or, alternatively, ~he polyurethane particles in the filter bed may have a cubic form, as may be obtained by physically cutting a body of polyurethane foam into small sized particles such as cubes having sides of 1/4 to 1 inch length. Suitable polyure~hane foam materials which have been employed successfully in practice have a cellular density of from 10 ~o 100 cells/inch. The true density of the poly-urethane particles in the filter bed should preferably be greater than about 1.34 lbs./ft. in order to provide structural integrity of the bed and to preclude floating of the polyurethane particles during the filtration step The polyurethane particles in the filter bed preferably have a solids loading capacity of at least one-half pound suspend-ed solids/ft polyurethane particles, in order to provide suitably high capacity for solids loading during the filtra-tion step. By way of example, a suitable foam polyurethane ;53~ 1 material for use in the process of the present invention may be shredded in form, with particle lengths on the order of 1 - 2 inches, 30 cells/linear inch, a particle thickness on the order of 0,25 inch, a true density (measur-ed without voids) of 1.77 lbs./ft. and a tensile strength of 23 5 psi.
During the filtration step, the volumetric flow velocity of the liquid containing suspended solids through the filter bed is desirably maintained between 1 and 10 gal/minute/ft of filter bed cross-sectional area, in order to provide adequate contacting of the liquid with the polyurethane particles i~ the filter bed without the occurr-ence of bypassing or other anomalous flow phenomens. After the filter bed is at least partially loaded with deposited solids, the flow of liquid through the filter bed is termin-ated. Subsequently, deposîted solids are removed from the discontinuous polyurethane particles in the filter bed, thereby renewing the filter bed for solids removal from the liquid containing suspended ~
,,-.. _ _ _ _ _ .. .... . . , .. . , . .. . . ...... _ _ _ ........ .
lU~l Prior to the renewal step, the flow of liquid through the filter bed 103 is terminated, as for example by closing the control valves 115 and 116 in lines 100 and 106 re-spectively. At the termination of flow of liquid through the filter bed, hold-up liquid will remain in the filter 103. In the renewal step, at least one bed volume of a regenera~ion liquid is added to the filtration vessel 102, to form a total volume of liquid in the filtration vessel comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from ~he termination of liquid flow through the filter bed. Figure 2 shows the sys~em of Figure 1 wherein the filtration vessel contains the afore-mentioned total volume of liquid. Prior to the addition of regeneration liquid to the filtration vessel, the filtration vessel will generally contain sufficient hold-up liquid to constitute a major fraction of a bed volume of liquid due ~o the high porosity of the fil~r bed of poly-urethane particles. For example, the porosity of the filter bed of polyurethane particles may be on the order of 80%, whereby the filtration vessel at the termination of liquid flow through the filter bed would contain 0.80 bed volume of hold-up liquid as interstitial liquid between the part-icles of polyurethane and liquid retained in the pores of the polyurethane particles in the filter bed.
As stat~d earlier herein, the term "bed volume"
means a unit volume of liquid which is equal to the volume . - 12 ~ 3~
of the f~lter ~ed Thus, if a fil~er bed is provided which ls two feet ln height in the filtration vessel, the addition of one bed volume of additional liquid (regeneration liquid) would resul~ in the provision of an admixture of polyurethane particles and liquid phase wherein the height of the liquid in the filtration vessel would be 4 ft.
The regeneration liquid added to the filtration vessel in the renewal step may comprise liquid containing suspended solids which is introduced to the filtration vessel in line 100, following which valve 115 in line 100 is closed. Alternatively, the regeneration liquid may comprise solids-depleted liquid, as for example clean water, when the liquid containing suspended solids is water.
The solids-depleted liquid may be introduced countercurrent-ly into the filtration vessel following termination of liquid flow through the filter bed by flow of the regenera-tion liquid through line 113 and countercurrently through that portion of line 106 which is directly benéath filtra-tion vessel 102. In the latter case, valve 114 in line 113 is open, while valves 115 in line 100 and valve 116 in line 106 are closed. During the normal filtration step, valve 114 is closed, while valves 115 and 116 are open.
The switching of the various respective valves may be carried out by a cycle time control system of a type well known to those ~killed in the art.
~ 6 After at least one bed volume of regeneration liquid has been added to the filtration vessel, as shown in Figure 2, all valves 114, 115 and 116 are closed. In preferred practice, the filter bed, as shown in Figure 1, occupies no more than one-half the volume of the fil~ration vessel, so as to allow for introduction of at least one bed volume of regeneration liquid to the filtration vessel. In the regeneratlon step, as mentioned, the filtration vessel contains a total volume of liquid comprising the regenera-tion liquid and the hold-up liquid in ~he filter bed re-sulting from the termination of liquid flow through the filter bed. In the general practice of the present in-vention, the hold-up liquid in the filter subsequent to the termination of liquid flow through the filter bed is intended to be construed broadly so as to include hold-up liquid in the filter bed, constituted by solids-depleted liquid remaining in the bed following the termination of liquid flow therethrough as well as to include the inter-stitial liquid between particles of polyurethane and the liquid which is re~ained in the pores of the polyurethane particles in the filter bed when the filter vessel is drain-ed of liquid following the termination of liquid flow through the filter bed and the hold-up liquid is replaced by a fractional bed volume of regeneration liquid. In other words, it is contemplated in the broad practice of ~he ~ 3~
present invention to completely drain $he filtration vessel of liquid following the filtration step and then to fill the fil~ration vessel with regeneration liquid to the desired extent such that a portion of the total volume of liquid replaces the hold-up liquid which was previously contained between the particles of polyurethane and in the pores of the polyurethane particles in the filter bed.
In this manner, the fractional bed volume of regeneration liquid which fills the pores and interstices of the filter bed becomes the hold-up liquid in the filter bed. Nonethe-less, it is generally preferred in practice to retain the hold-up liquid in the filter bed resulting from the termin-ation o liquid flow through the filter bed in order to min-imize the filter bed regeneration time and to simpl~fy the regeneration procedure.
In the system as shown in Figure 2, after the regeneration liquid had been introduced to the filtration vessel to form a total volume of liquid comprising the re-generation liquid and the hold-up liquid therein, the filter bed of discontinuous polyurethane particles having the solids deposited thereon is mechanically mixed to cause deposited solids to disengage from the discontinuous poly-urethane particles and pass into the ~otal liquid volume, thereby forming solids-enriched liquid. This is carried out by energizing the motor drive means 117 which is 1 ~ O ~ 1 ~ 53~
connected by rotating shaft member 118 to rotating impeller means 119. In this manner, the filter ~ed is mechanically mixed by agitating the polyurethane particles in the total liquid volume in the filtration vessel. Such agitation causes disengagement of the deposited solids from the poly-urethane particles in the bed and forms the aforemen~ioned solids-enriched liquid in the filtration vessel. After a suitable period of agitation, which for example may be 1 - 3 minutes,when disengagement of deposited solids from the polyurethane particles has been effected, the motor drive means 117 is deenergized and the solids-enriched liquid is discharged from the filtration vessel in line 106 by opening of valve 116; The solids-enriched liquid in line 106 may be passed to further treatment and/or end use facilities, such as sludge drying beds. After the solids-enriched liquid is fully discharged from the filtration vessel, the filter bed is fully renewed for the subsequent filtration s~ep, which may be initiated by opening valve 115 in feed liquid line 100 to admit liquid containing sus-pended solids to the filtration vessel 102 for filtration therein as earlier described.
It was stated earlier herein that the regenera-tion liquid preferably comprises between one and two bed volumes of liquid. Such volumetric amounts of regenera-tion liquid are satisEactory in the broad practice of the ~ 3~
present invention to fully regenerate the polyurethane particle filter bed. By way of example, experience has shown that a 30 cell per linear inch polyurethane foam filter bed can be satisfactorily regenerated in one bed volume of regeneration liquid (in addition to the hold-up liquid in the filtration vessel.) A 60 cell per linear inch polyurethane foam filter bed, on the other hand, has been found to require 1.6 bed volumes of regeneration liquid (in addition to the hold-up liquid in the filtra-tion vessel) for efficient regeneration. This difference is due to the fact that the 60 cell polyurethane foam is less dense than the 30 cell polyurethane foam and thus the former requires a correspondingly greater volume for mechan-ical mixing in the regeneration step.
Referring now to Figure 3, ~here is shown a schematic diagram of another process system in which the process of the instant invention can be carried out. Liquid containing suspended solids is introduced into the system in line 200 having con~rol valve 215 disposed therein from which it is distributed by the distributor means 201 a~ the upper end of the filtration vessel 202 to the filter bed 203 of discontinuous polyurethane particles contained in the filtration vessel. The filter bed of discontinuous poly-urethane particles has an u~per inlet end and a lower dis-charge end, with the latter resting on support structure 204~ which provides a lower plenum space 205 for collec~ion ~ 53~
of purified llquid from the filter bed. The liquid contain ing suspended solids is flowed through the filter bed in the filtration vessel for deposi~ion of the solids on the polyurethane particles to form solids-depleted liquid. The solids-depleted liquid is discharged from the filtration vessel 202 in line 206. During the normal filtration step valve 215 in line 200 is open and valve 209 in line 208 is closed.
From line 206, solids-depleted liquid is passed to the downstream filter bed 237 for final effluent polish-ing of the liquid. The do~lstream filter bed 237 may be a conventional sand filter or of a mixed media type. The downstream bed 237 is contained in vessel 236 and receives liquid from line 206 through distributor means 23~, which may be of a type similar to that employed in filtration vessel 202. The liquid flowing through the downstream filter bed 237 is discharged therefrom in line 238 and passed to reeeiving waters and/or other desired end use.
The above-described filtration step is continued until the filter bed is at least partially loaded with deposited solids, at which point the flow of liquid through the filter bed is terminated. The filter bed of polyurethane particles is now ready for renewal by removal of deposited solids from the discontinuous polyurethane particles of the bed, thereby re-establishing the capability of the filter bed for solids removal from the liquid cont~ining suspended ~ 3 solids.
In the renewal step, at least one bed volume of regeneration liquid is added to the filtration vessel 202. The filter bed of discontinuous polyurethane particles having the solids deposited thereon is then mechanically mixed by agitation by energizing motor drive means 217 which is connected by shaft member 218 to impeller means 219. Mixing agitation is carried out for a suitable time, as for example 1 - 3 minutes, in a total volume of liquid comprising the regeneration liquid and the hold-up liquid in the filter bed resulting from termination oE liquid through the filter bed~ to cause deposited solids to dis-engage rom the discontin~ous polyurethane particles and pass into the total liquid volume, ~hereby forming solids-enriched liquid. At this point valve 209 in line 208 is opened and the solids-enriched liquid is discharge~ from ; the filtration vessel in line 208. Subsequent to the dis-charge of solids-enriched liquid from the filtration vessel 202, the filter bed 203 in the vessel is renewed and ready for the normal fil~ration step. The second filter bed 237 may be regenerated in any suitable manner such as by con-ventional back-washing.
The advantages of the present invention are illustrated in the ollowing example.
- 19 ~
~ S3 EXAMPLE
A comparative performance evaluation was carried out on filter beds regenerated by back-washing and by agitation mixing in manner of the present invention. In the evaluation, two filter beds were arranged in parallel flow relationship and were arranged to filter identical respective portions of a common flow of solids-containing waste water. Each bed was contained in a glass column having an inner diameter of 14 centimeters. Each con~ained 75 grams of a 60 cell per linear inch shredded polyurethane foam of approximately 95% porosity which formed filter beds in the respective columns each 23 centimeters in height, at a packing density of 30 grams of polyurethane foam per liter of filter bed volume.
The respective filter beds each processed a flow of 200 milliliters of suspended solids containing waste water per minute. Four separate runs were made with re-generation between successive filtration steps and the fourth run was considered as representative of steady state operating conditions. Each filtration step was carried out for 8 hours. Subsequent to the termination of the filtration step, one of the filter beds was re-generated by back-washing and the other was regenerated by agitation mixing in the manner of the present invention.
In the back-washi~g regeneration step for the ~ 3~
first fil~er bed, clean water was flowed as the back-wash medium through the filter bed in a direction counter-current to the down flow direction of liquid flow through the filter bed during the normal filtration step. In the back-washing step, the back-washing flow rate was 18 gallons per minute per ft. of filter bed cross-sectional area. Re-generation was carried out for 5 minutes, at which ~ime the effluent back-wash liquid appeared to be relatively solids-iree .
In the filter bed regenerated in accordance with the method of the present invention, one bed volume of regeneration liquid ~clean water) was added to the filtra-tion vessel and the filter bed was mechanically mixed in a total volume of liquid comprising the one additional bed volume of regeneration liquid and the hold-up liquid in the filter bed resulting from the termination o~ liquid flow through the filter bed. Following the addition of the re-generation liquid, the filter bed was mixed for two minutes by an impeller comprising four 45 pitched blades. The diameter of ~he mixing impeller was approximately 5 centi-meters and the impeller was rotated dur;ng the mixing agita~
tion s~ep at a rotstional speed on the order 100 - 200 rpm.
The mixing agitation was then terminated and the bed was drained of liquid. The filter bed was then refilled wi~h two additional bed volumes of clean water and again mechan-ically mixed for two minutes. The mixing agitation was again terminated and the bed returned to the filtration operation.
~ 6 Comparative performance data for the respective regener~ion modes are set forth below in Table I.
_ Table I _ _ _ _ _ Comparative Performance of Filter Beds Regenerated by Back-washing and by Agitation Mixin~
Parameter ~ D~tion Method Backwashing Agitation Mixing . . _ ,_ Total Regeneration Liquid Volume, gal. 14 4.5 Solids initially on filter bed PmS 18 18 _ , _ Solids on filter bed after regeneration, ~ms 5 0O5 .~ . _ _ _ Solids re~oved, % 72% 97.5~O
As shown by the data, the backwashing regeneration method required 14 gals. of total regenerativn liquid, whereas the agitation mixing regeneration method of this invention re-quired only 4.5 gals. (note: the total regeneration liquid volume listed in the Table for the agitation mixing method comprises the added bed volumes of regeneration liquid and the hold-up liquid in the filter bed contained in ~he pores and interstices of the filter bed~. As also shown by the - data, the back-washing regeneration method yielded only a 72% solids removal from the filter bed, despite the large volume of regeneration liquid employed, while the agitation mixing regeneration method of the present invention resulted in a 97.5/0 solids removal.
Although preferred embodiment of the invention have been described in detail, it is to be recognized that other embodiments only with modification of the disclosed features are contemplated as being within the scope of the invention.
Claims (18)
1. In a process for removal of solids from a liquid containing suspended solids including the steps of:
(a) providing a filtration vessel containing a filter bed of discontinuous polyurethane particles;
(b) flowing said liquid containing suspended solids through said filter bed in said filtration vessel for deposition of said solids on said polyurethane particles to form solids-depleted liquid, and discharging solids-depleted liquid from said filtration vessel, until said filter bed is at least partially loaded with deposited solids;
(c) terminating the flow of liquid through said filter bed; and (d) removing deposited solids from the dis-continuous polyurethane particles in said filter bed, there-by renewing said filter bed for solids removal from said liquid containing suspended solids, the improvement wherein the removal of deposited solids from the discontinuous poly-urethane particles of said filter bed is carried out by adding at least one bed volume of a regeneration liquid to said filtration vessel and mechanically mixing said filter bed of discontinuous polyurethane particles having said solids deposited thereon in a total volume of liquid com-prising said regeneration liquid and the hold-up liquid in said filter bed resulting from said termination of liquid flow through said filter bed to cause deposited solids to disengage from said discontinuous polyurethane particles and pass into said total liquid volume, thereby forming solids-enriched liquid, and discharging said solids-enriched liquid from said filtration vessel.
(a) providing a filtration vessel containing a filter bed of discontinuous polyurethane particles;
(b) flowing said liquid containing suspended solids through said filter bed in said filtration vessel for deposition of said solids on said polyurethane particles to form solids-depleted liquid, and discharging solids-depleted liquid from said filtration vessel, until said filter bed is at least partially loaded with deposited solids;
(c) terminating the flow of liquid through said filter bed; and (d) removing deposited solids from the dis-continuous polyurethane particles in said filter bed, there-by renewing said filter bed for solids removal from said liquid containing suspended solids, the improvement wherein the removal of deposited solids from the discontinuous poly-urethane particles of said filter bed is carried out by adding at least one bed volume of a regeneration liquid to said filtration vessel and mechanically mixing said filter bed of discontinuous polyurethane particles having said solids deposited thereon in a total volume of liquid com-prising said regeneration liquid and the hold-up liquid in said filter bed resulting from said termination of liquid flow through said filter bed to cause deposited solids to disengage from said discontinuous polyurethane particles and pass into said total liquid volume, thereby forming solids-enriched liquid, and discharging said solids-enriched liquid from said filtration vessel.
2. A process according to claim 1 wherein said filter bed occupies no more than one-half the volume of said filtration vessel.
3. A process according to claim 2 wherein said mechanical mixing comprises mechanically agitating said filter bed of polyurethane particles.
4. A process according to claim 1 wherein said regeneration liquid comprises between one and two bed vol-ume of liquid,
5, A process according to claim 1 wherein said regeneration liquid comprises solids-depleted liquid.
6. A process according to claim 1 wherein said regeneration liquid comprises liquid containing suspended solids.
7. A process according to claim 1 wherein said discontinuous polyurethane is in the form of shredded non-uniformly sized particles.
8. A process according to claim 1 wherein said discontinuous polyurethane has a cellular density of from 10 to 100 cells/inch.
9. A process according to claim 1 wherein said liquid containing suspended solids is water.
10. A process according to claim 1 wherein the volumetric flow velocity of said liquid containing sus-pended solids through said filter bed is between 1 and 10 gal/min/ft2 of filter bed cross-sectional area.
11. A process according to claim 1 wherein the true density of the polyurethane particles in said filter bed is greater than 1.34 lbs/ft3.
12. A process according to claim 1 wherein the polyurethane particles in said filter bed have a solids loading capacity of at least 0.5 lb. suspended solids/ft3 polyurethane particles.
13. A process according to claim 1 wherein the polyurethane particles in said filter bed have a cubic form.
14. A process according to claim 1 wherein the solids-depleted liquid discharged from said filtration vessel is passed through a second filter bed for final effluent polishing of said liquid.
15. A process according to claim 1 wherein said regeneration liquid comprises solids-depleted liquid intro-duced countercurrently into said filtration vessel following termination of liquid flow through said filter bed.
16. In a process for removal of solids from a liquid containing suspended solids including the steps of:
(a) providing a filtration vessel containing a filter bed of discontinuous polyurethane particles;
(b) flowing said liquid containing suspended solids through said filter bed in said filtration vessel for deposition of said solids on said polyurethane particles to form solids-depleted liquid, and discharging solids-depleted liquid from said filtration vessel, until said filter bed is at least partially loaded with deposited solids;
(c) terminating the flow of liquid through said filter bed; and (d) removing deposited solids from the dis-continuous polyurethane particles in said filter bed, there-by renewing said filter bed for solids removal from said liquid containing suspended solids, the improvement wherein the re-moval of deposited solids from the discontinuous polyurethane particles of said filter bed is carried out by adding a re-generation liquid to said filtration vessel and mechanically mixing said filter bed of discontinuous polyurethane particles having said solids deposited thereon in a total volume of liquid at least equal to the volume of hold-up liquid in said filter bed at the termination of liquid flow through said filter bed and one bed volume of additional liquid to cause deposited solids to disengage from said discontinuous polyurethane particles and pass into said total liquid volume, thereby forming solids-enriched liquid, and discharging said solids-enriched liquid from said filtration vessel.
(a) providing a filtration vessel containing a filter bed of discontinuous polyurethane particles;
(b) flowing said liquid containing suspended solids through said filter bed in said filtration vessel for deposition of said solids on said polyurethane particles to form solids-depleted liquid, and discharging solids-depleted liquid from said filtration vessel, until said filter bed is at least partially loaded with deposited solids;
(c) terminating the flow of liquid through said filter bed; and (d) removing deposited solids from the dis-continuous polyurethane particles in said filter bed, there-by renewing said filter bed for solids removal from said liquid containing suspended solids, the improvement wherein the re-moval of deposited solids from the discontinuous polyurethane particles of said filter bed is carried out by adding a re-generation liquid to said filtration vessel and mechanically mixing said filter bed of discontinuous polyurethane particles having said solids deposited thereon in a total volume of liquid at least equal to the volume of hold-up liquid in said filter bed at the termination of liquid flow through said filter bed and one bed volume of additional liquid to cause deposited solids to disengage from said discontinuous polyurethane particles and pass into said total liquid volume, thereby forming solids-enriched liquid, and discharging said solids-enriched liquid from said filtration vessel.
17. A process according to claim 16 wherein said filter vessel is drained of liquid following the termina-tion of liquid flow through said filter bed and the hold-up liquid resulting from the termination of liquid flow through the filter bed is replaced by a fractional bed vol-ume of regeneration liquid.
18. A process according to claim 17 wherein said regeneration liquid comprises between one and two bed vol-ume of liquid in addition to a fractional bed volume of liquid equal to the volume of hold-up liquid in said filter bed resulting from the termination of liquid flow there-through.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000326251A CA1116536A (en) | 1979-04-24 | 1979-04-24 | Process for removal of suspended solids from liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000326251A CA1116536A (en) | 1979-04-24 | 1979-04-24 | Process for removal of suspended solids from liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1116536A true CA1116536A (en) | 1982-01-19 |
Family
ID=4114055
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000326251A Expired CA1116536A (en) | 1979-04-24 | 1979-04-24 | Process for removal of suspended solids from liquid |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1116536A (en) |
-
1979
- 1979-04-24 CA CA000326251A patent/CA1116536A/en not_active Expired
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