Vacuum Ceramic Disk Filters for Mining Tailings
A ceramic disk filter is worth evaluating for tailings when the slurry forms a coherent cake on the ceramic sectors, releases reliably, and gives filtrate suitable for the planned destination. Verify those conditions on the feed the machine will actually see.
Check Whether the Slurry Can Run Through the Ceramic Cycle
As the disk rotates through the slurry, vacuum draws liquid through the porous ceramic sectors and solids build up on their surface. The cake continues to dewater as the disk rises above the slurry. The filter then discharges the cake, and the cleaning system helps restore the sectors for subsequent cycles. Suitability depends on what happens across all four stages. Good filtrate on the first pass can coexist with low solids output or poor cake release.
Take samples from the proposed filter feed point, typically thickener underflow where a thickener is installed. Include a normal sample and credible difficult feeds, such as periods with a larger fine fraction, a different ore blend or a change in reagent carryover. Record solids by weight, particle-size distribution, relevant chemistry and temperature. If a test uses a different feed concentration or conditioning method from the planned plant, record the change and check whether the plant can maintain it. See tailings sampling by ore type.
Read the Test Results Before Choosing the Filter
| What you observe | What to check next | What it means for selection |
|---|---|---|
| Uniform cake forms and releases repeatedly | Record dry solids per unit of active area and time, wet-basis cake moisture, and filtrate quality. Check the same measures on difficult feed. | Keep ceramic on the shortlist if the sustained rate, cake handover and filtrate all meet the duty. |
| Rate starts high and then falls | Log feed solids, filtrate flow and vacuum together. Check the rate after cleaning. A falling rate can come from changes in feed or the vacuum system as well as sector fouling. | If cleanings restore the rate, account for their frequency and duration. If recovery is weak or the resulting output is too low, compare trial cloths on the same feed. |
| Cake is patchy, smears or sticks | Check feed stability, formation time and the discharge setup. Observe the cake at the chute as well as at the sector. | If stable feed and realistic settings still give poor release, compare cloth media and their discharge arrangements. Check how both cakes behave on transfer. |
| Cake releases but is too wet for the receiver | Compare moisture against drying time and output. Use the same wet-basis measurement for all trials, as a percentage of total wet cake mass. | If the vacuum route misses the target or needs too much drying time to meet throughput, compare a membrane press on the same representative feed. |
| Filtrate misses the return-water limit | Separate startup from steady samples. Check suspended solids against the receiving process limit and verify the relevant dissolved chemistry separately. | Consider an alternate medium or separate routing for high-solids streams. Where dissolved chemistry is the constraint, evaluate the receiving circuit or separate treatment. |
Testwork on Serra do Sapo iron ore tailings showed why moisture and rate need to be read together. On thickened, coagulated samples, adding ultrafines lowered the ceramic filtration rate even though cake moisture could still meet the study limit. The study obtained measurable results on its ultrafine-only sample with a filter press. Use this example to plan which feed blends to test. See the UFMG study on iron ore tailings filtration, section 5.6 and the abstract.
Size From Sustained Output, Then Check the Plant Interfaces
Use a rate from repeated cycles on representative feed. For a first sizing check, divide the required dry-solids load in kilograms per hour by the net rate in kilograms of dry solids per square metre per hour on the same time basis. A hypothetical load of 12,000 kilograms per hour at a net rate of 150 kilograms per square metre per hour gives 80 square metres of active area. This is an arithmetic example. Confirm the rate and scale-up with testwork, then check available machine sizes, the difficult-feed case and any required standby capacity. Avoid deducting routine cleaning time twice if the net rate already includes it.
Move beyond a single bench test if feed variability or cleaning recovery drives the size, or if a bench test cannot represent continuous discharge. Agree what the pilot must demonstrate, how long it should run and which difficult feeds to include. If the proposed configuration cannot sustain both the solids load and the cake requirement, compare the cloth disc vacuum route ou un filtre-presse à membrane on matched feed and a common operating basis.
Configure the Ceramic Filter Around the Feed and Cleaning Duty
PORVOO can configure filtration area, sector selection, discharge and auxiliaries for the project. If flow declines during a trial, check feed and vacuum stability first, then record the filtration rate before and after each regeneration step. This shows whether the cleaning sequence can recover enough capacity for the planned duty.
- Backwash and regeneration: Review backwash with suitable service water or filtrate. Where trials show that backwash alone does not restore enough flow, evaluate periodic ultrasonic or compatible chemical cleaning. Confirm water quality, media and seal compatibility, drainage and the time taken out of production before specifying the sequence.
- Controls and retrofit: Agree which functions the local panel should handle and which signals go to the plant control system. For example, specify how low feed level or loss of vacuum is detected and what the filter should do. Check sector replacement access, scraper clearance and the connection to the existing chute before finalizing the layout.
What to Ask for in a Ceramic Disk Filter Quote
Ask each supplier to quote against the same feed range and handover conditions. A proposed filtration area is easier to compare when the quote states which test and operating assumptions support it, and which parts of the system the price covers.
| Article | What the quote should state |
|---|---|
| Active area and number of filters | Area per unit, units in service and any standby unit. Ask which feed and sustained rate support the proposed size, and whether cleaning time is included. |
| Sectors and discharge | Proposed sector specification, scraper arrangement and discharge elevation. Check how cake reaches the chute or conveyor and which sectors and wear parts are included as spares. |
| Feed, vacuum and filtrate | Required feed flow, solids range and available head. Mark who supplies the feed tank and agitator, vacuum equipment, receiver and piping for filtrate return or diversion. |
| Cleaning, controls and access | Proposed regeneration sequence, utility and drainage needs, and controls and interlocks. Ask for a layout showing clearance for drive service, scraper inspection and sector removal. |
| Conditions d'acceptation | Feed conditions, measurement window and agreed criteria for dry-solids output, cake handover and filtrate. Identify the checks that still need pilot or site confirmation. |
Utilisez le vacuum ceramic disk filter product page to review the equipment construction. The testwork page covers sample preparation, and the engineering scope guide helps assign equipment, utilities and site responsibilities.
Discuss Your Project
Send normal and peak dry-solids load, slurry solids by weight, sample points, and any particle-size or chemistry data. Include cake moisture and handling requirements, filtrate limits and operating hours. If you already run a filter, add the medium type, the rate before and after cleaning, any problems with release, and the current discharge layout. These details help define the first trial and the conditions for comparing a second route.
