NEWS
Focus On High-Quality Silicate (Ceramic) Materials
Maximizing Spray Dryer Output: How Slurry Solid Content and Atomization Affect Granule Morphology
By the Goway Chemical Technical Team • Published June 2026 • 18-minute read
Spray dryer throughput in ceramic tile production is fundamentally limited by the evaporation capacity required to convert slurry into dried granules. The single most effective lever for increasing output without capital investment is raising slurry solid content — each 1 percentage point increase reduces water evaporation load by approximately 3–5%, directly translating into higher powder production rate.
However, solid content cannot be raised arbitrarily. It is constrained by slurry rheology: at higher solids, viscosity rises exponentially, impacting pumpability and — critically — atomization quality. The droplet size distribution formed during atomization determines granule morphology (sphericity, hollow fraction, surface texture, particle size distribution), which in turn governs powder flow, die filling uniformity, pressing compaction, green density, and ultimately fired tile quality.
The engineering challenge is to coordinate slurry-side optimization (deflocculant selection, solid content elevation) with atomization-side tuning (nozzle type, pressure/RPM, feed rate) to achieve the maximum throughput that still produces granules with acceptable pressing performance.
Key Facts at a Glance
- Throughput lever: Each +1% solid content (dry basis) reduces water evaporation load by ~3–5% per tonne of output (typical engineering reference value; actual depends on dryer thermal efficiency and fuel type)
- Typical operating range: Ceramic tile body slurry operates at 62–68% solid content; optimized systems with effective deflocculants may reach 68–70+% (P3: Industry process reference range)
- Atomization ceiling: Practical slurry viscosity for good atomization typically ~500–1,200 mPa·s at nozzle shear rates (P3: Typical engineering experience range; varies with atomizer design)
- Droplet size estimation (pressure nozzle): D50 ∝ P−0.3 × d0.5 — where P is pressure (bar), d is orifice diameter; higher pressure and smaller orifice each reduce median droplet size (P3: Simplified empirical correlation from spray drying engineering practice; Ref: Masters, Spray Drying Handbook, for complete model)
- Droplet size estimation (rotary atomizer): D50 ∝ (1/N)0.8 — where N is wheel speed (RPM); higher RPM produces finer, more uniform droplets (P3: Simplified empirical correlation; Ref: Masters, Spray Drying Handbook, for complete model)
- Morphology impact on pressing: Spherical, surface-smooth granules flow freely and fill dies uniformly; fragmented/hollow granules cause density variation, lamination risk, and inconsistent green strength
- PSD target: Ideal spray-dried powder contains a continuous particle size distribution with fines (<63 μm), medium (63–250 μm), and coarse (>250 μm) fractions in balanced proportions for maximum packing density during pressing (P3: Typical ceramic body pressing reference)
§1 The Causal Chain: Slurry → Atomization → Granule → Pressing
Spray dryer performance cannot be optimized by tuning any single variable in isolation. Each adjustment in the slurry preparation stage propagates through atomization and drying, ultimately appearing as a measurable change in the pressing line. Understanding this complete causal chain is the foundation of systematic optimization.
1.1 Slurry Properties: The Starting Point
The slurry leaving the ball mill determines everything downstream. Three properties matter most for spray drying:
Water Evaporation Load
Determines how much water the dryer must remove per tonne of powder output. This is the primary throughput lever.
Typical: 62–68%Atomization Quality
Controls droplet breakup during atomization. High-viscosity slurry produces coarse, irregular droplets or filaments.
Target: 500–1,200 mPa·s at nozzle shearFlow Stability
Thixotropic slurries gel during pauses and thin under shear; dilatant slurries thicken under shear. Both cause atomization instability.
Preferred: Near-NewtonianDispersion Mechanism
Electrostatic (STPP-type) vs. electrosteric (polyacrylate-type) stabilization determines the solid content ceiling.
Dosage: 0.3–0.8% dry body weightEvaporation Load Calculation (Illustrative)
For a spray dryer producing 10 tonnes/hour of powder, the water evaporation demand changes dramatically with solid content:
This is a mass-balance calculation based on the definition of solid content (dry weight / total weight). Actual throughput gain depends on dryer thermal capacity and inlet/outlet air temperature constraints. Equivalent to approximately 30% potential throughput increase, assuming the dryer can accept the reduced water load at current thermal input. (P3: Engineering calculation, verified by mass balance)
1.2 Viscosity: The Critical Constraint
Raising solid content inevitably increases slurry viscosity. The relationship is nonlinear — viscosity climbs gently at moderate solids, then rises sharply as particle packing approaches a critical threshold:
The effective deflocculant (Ceramic Deflocculant / STPP Replacement) determines whether this viscosity rise is manageable at elevated solids. Electrosteric dispersants (combining electrostatic charge repulsion with polymer steric hindrance) typically maintain a lower viscosity at a given solid content than purely electrostatic dispersants (e.g., STPP), because steric stabilization prevents clay platelet face-to-edge flocculation even at high particle packing densities. (P3: Established ceramic dispersion mechanism; Ref: Reed, J.S., Principles of Ceramics Processing, 2nd ed.)
For further detail on viscosity reduction strategies, the companion guide on Reduce Ceramic Slurry Viscosity covers deflocculant selection and dosage optimization. Additionally, efficient milling in the Ball Mill Energy & Grinding Aids stage directly affects the particle size distribution entering the spray dryer — finer, more uniform grinding reduces water demand per unit solid content.
§2 Slurry-Side Optimization: Deflocculants and Solid Content
2.1 The Deflocculant's Role in Solid Content Elevation
A ceramic slurry at high solid content is a concentrated suspension. Without effective dispersion, clay platelets flocculate, trapping water in inter-particle voids and raising the apparent viscosity beyond pumpable limits. The deflocculant's function is to maintain particle separation, minimizing the water immobilized in floc structures and making that water available as free liquid for flow.
Switch to Electrosteric Deflocculant
Polyacrylate-based ceramic deflocculants provide both charge repulsion (electrostatic) and polymer chain steric hindrance. This dual mechanism maintains dispersion at higher particle packing densities than purely electrostatic STPP-type deflocculants.
Optimize Deflocculant Dosage
Each deflocculant-mineral system has an optimum dosage. Under-dosing leaves flocculated structures; over-dosing can cause re-flocculation through ionic strength effects or wasted cost.
Reduce Ball Clay Proportion
Ball clays have intrinsically high water demand due to fine particle size and platelet morphology. Reformulating the body to reduce ball clay and increase kaolin or processed clay can lower water demand, enabling higher solid content.
Optimize Milling Particle Size Distribution
A broader particle size distribution packs more efficiently than a narrow one, reducing the interstitial void volume that must be filled with water. Ball mill residence time and grinding media charge directly affect this.
The specific viscosity vs. solid content curves for Goway deflocculant products (FG-2017, FG-MK03, FG-N203B, FG-SL01A) at different slurry formulations are not available in the current Technical Data Sheet revision. The performance gains cited above are engineering reference ranges from industry practice. For product-specific rheology data at your target solid content and raw material composition, a laboratory compatibility trial with your slurry is recommended. Contact Goway's technical team with your raw material mix and current deflocculant for a customized solid content elevation assessment.
2.2 Solid Content Elevation Protocol (Incremental Approach)
Establish Baseline at Current Solids
Measure viscosity (Brookfield or Ford Cup), density, and flow time at current production solid content. Record deflocculant type and dosage.
Incremental Solid Content Increase (+2%)
Prepare slurry at +2 percentage points higher solids (e.g., from 64% to 66%). Adjust deflocculant dosage to maintain target viscosity. If target viscosity cannot be achieved, adjust deflocculant dosage using a 5-point curve (current dosage, +0.05%, +0.10%, +0.15%, +0.20%).
Atomization Check
Spray a small batch through the production or pilot dryer. Measure droplet size qualitatively (visual spray pattern) and collect dried granules for morphology analysis (PSD by sieve analysis, SEM morphology check, bulk density, flowability).
Press Trial
Press tiles with the new granules. Verify die fill time, green density (by dimension and weight), green strength (3-point bending), and visual inspection for lamination or density variation. Compare against baseline.
Iterate or Validate
If pressing quality meets specification, validate at production scale. If not, reduce solid content incrementally or adjust atomization parameters before retrying.
§3 Atomization-Side Optimization: Nozzles, Pressure, and RPM
3.1 Pressure Nozzle vs. Rotary Atomizer: Fundamental Differences
The two dominant atomizer types in ceramic spray drying produce distinct granule morphologies because they create droplets through fundamentally different mechanisms:
Slurry is forced through a small orifice under high pressure (typically 20–60 bar). The liquid jet destabilizes into ligaments, which break into droplets. Droplet size is controlled primarily by orifice diameter and pressure drop.
- Narrower particle size distribution
- Higher bulk density granules
- Greater risk of hollow spheres at high inlet T
- Orifice wear changes PSD over time
Slurry is fed onto a spinning wheel or disc (typically 8,000–18,000 RPM). Centrifugal force spreads the slurry into a thin film, which breaks into droplets at the wheel periphery. Droplet size is controlled primarily by wheel speed and feed rate.
- Wider particle size distribution
- More spherical, fewer hollow shells
- Lower sensitivity to viscosity changes
- Better tolerance for abrasive slurries
Parameter ranges are typical for ceramic spray drying applications. Specific values depend on dryer manufacturer and model. (P2: Ref: Masters, K., Spray Drying Handbook, 4th ed.; GEA Niro and SiccaDania technical literature; P3: Typical ceramic industry operating ranges)
3.2 Droplet Size Estimation and Control
Rotary atomizer: D50 (μm) ≈ kr · (1 / N)0.8 · (σ / ρ · R)0.5
P = atomization pressure (bar) | d = orifice diameter (mm)
N = wheel rotational speed (RPM) | R = wheel radius (m)
σ = slurry surface tension (N/m) | ρ = slurry density (kg/m³)
kp, kr = empirical constants (system-specific; determined by calibration)
These simplified correlations illustrate the key tuning principle: increasing atomization energy (higher pressure or RPM) reduces median droplet size, producing finer granules, while increasing orifice diameter or reducing wheel speed coarsens the product. However, the system-specific constant means absolute prediction is unreliable without calibration — a pilot trial at the target condition is always required.
3.3 Parameter Tuning Guide
| Parameter | Effect on D50 | Effect on Distribution Width | Effect on Hollow Fraction | Practical Adjustment |
|---|---|---|---|---|
| Atomization pressure ↑ (nozzle) | Decreases | Narrows slightly | May increase (finer droplets dry faster, form shells) | +5 bar increments; monitor spray cone angle stability |
| Nozzle orifice ↑ | Increases | Widens | Decreases (larger droplets dry slower, denser core) | Inspect orifice for wear; replace if diameter deviates >5% from nominal |
| Wheel speed ↑ (rotary) | Decreases | Narrows | Slight increase at very high RPM | +500 RPM increments; verify motor load within rating |
| Feed rate ↑ (rotary) | Increases | Widens | Decreases (thicker film on wheel) | Match to evaporation capacity; excess feed causes wet powder |
| Slurry viscosity ↑ | Increases | Widens | Variable — depends on surface tension change | Reduce via deflocculant adjustment or decrease solids |
| Inlet air temperature ↑ | No direct effect on droplet | N/A | Increases (rapid shell formation traps vapor) | Balance with evaporation capacity; +20°C increments |
P3: Directional effects are engineering reference guidelines based on spray drying process principles (Ref: Masters, Spray Drying Handbook). Magnitude of each effect is system-specific and must be verified by trial. Effects on D50 assume other parameters held constant.
3.4 Nozzle Wear Monitoring
For pressure nozzle systems, one of the most common but underdiagnosed causes of gradual PSD drift is orifice wear. The ceramic slurry is abrasive, and even hardened nozzle inserts erode over time. A worn orifice has a larger effective diameter, producing coarser granules with a wider distribution — a shift that may go unnoticed for weeks while pressing rejects accumulate.
Track the pressure required to maintain a constant feed rate through each nozzle. When the required pressure drops by more than 10% from the baseline (clean nozzle, same slurry), the orifice has worn and should be replaced. Alternatively, measure granule D50 from a sieve analysis weekly — a shift of more than 15% in D50 at constant atomization parameters indicates nozzle wear. (P3: Typical maintenance monitoring practice)
§4 Granule Morphology and Pressing Performance
4.1 How Granule Shape, Size, and Density Drive Pressing Behavior
The spray dryer's output is not the final product. The granules must be transported, stored, and — most critically — pressed into a green body. Every morphological characteristic of the granule population influences the pressing process:
| Granule Property | Pressing Impact | Measurement Method | Optimization Direction |
|---|---|---|---|
| Sphericity | Spherical granules flow freely; irregular shapes interlock, causing die fill variation and density gradients across the pressed part | Optical microscopy / SEM imaging (qualitative); sphericity index via image analysis | Target spherical via optimal droplet drying: avoid excessive inlet temperature (rapid shell), maintain moderate drying rate |
| Particle Size Distribution (PSD) | Continuous, broad PSD packs to higher green density. Narrow PSD leaves inter-granule voids. Excessive fines (<63 μm) cause die sticking; excessive coarse (>400 μm) cause lamination | Sieve analysis (63, 125, 250, 400, 500 μm mesh stack); calculate span = (D90 − D10) / D50 | Rotary atomizers naturally produce wider PSD. With pressure nozzles, consider multi-nozzle arrays with staggered orifice sizes |
| Bulk Density | Higher bulk density granules pack more mass per die volume, producing higher green density at a given pressing pressure. Low bulk density (hollow shells) causes spring-back and lamination | Graduated cylinder method (tap density or free-flow density); ASTM B212 / ISO 3923 | Reduce hollow fraction (lower inlet temperature / higher solids); coarser granules typically have higher bulk density |
| Hollow Shell Fraction | Hollow granules collapse during pressing, releasing trapped air that can form inter-layer defects. Severely hollow shells do not compact and leave porosity after pressing | SEM cross-section; crush test (force required to break individual granules); apparent vs. true density comparison | Reduce inlet air temperature (slower shell formation); increase solid content (less water to evaporate from each droplet reduces shell inflation) |
| Surface Texture | Smooth granules have lower inter-particle friction, better flow, and more uniform die fill. Rough or dimpled surfaces increase friction and cause arching in feed hoppers | SEM imaging; Hall flowmeter funnel test time | Smooth surface is favored by moderate drying rate, moderate solid content, and rotary atomization |
| Residual Moisture | 0.5–2% residual moisture is necessary for pressing — it acts as a lubricant during particle rearrangement. Insufficient moisture (<0.3%) causes high ejection force and die wear. Excessive (>3%) causes sticking | Moisture balance / halogen analyzer; oven drying at 110°C to constant weight | Adjust outlet air temperature or feed rate to target 0.5–1.5% outlet moisture for ceramic tile body granules |
P3: Engineering reference ranges for ceramic tile body spray-dried granules. Specific targets depend on body formulation, press type, and tile format. (Ref: Reed, J.S., Principles of Ceramics Processing; industry processing reference)
4.2 The "Goldilocks" Granule Distribution
No single granule size is optimal for pressing. A continuous distribution containing fines, medium, and coarse fractions packs most efficiently because small particles fill the interstices between larger ones:
| Fraction | Sieve Range (μm) | Ideal Proportion | Function in Pressing |
|---|---|---|---|
| Fines | <63 | 5–15% | Fill interstitial voids; reduce green porosity. Excess fines cause die sticking and dust generation |
| Fine-Medium | 63–125 | 15–25% | Bridge between fines and medium fractions; improve packing efficiency |
| Medium | 125–250 | 30–40% | Core particle fraction; provides bulk of die fill mass |
| Medium-Coarse | 250–400 | 15–25% | Prevent over-packing and improve flow; maintain open structure during initial compaction |
| Coarse | 400–630 | 5–10% | Improve die fill flow; excess causes lamination defects |
P3: Typical proportional reference ranges for ceramic tile body powder. Actual targets depend on tile format (large format tiles may benefit from slightly coarser distribution), press type (isostatic vs. uniaxial), and body plasticity. Verification by pressing trial is recommended.
4.3 Morphology Defects and Pressing Consequences
| Granule Defect | Pressing Symptom | Root Cause | Primary Action |
|---|---|---|---|
| High hollow shell fraction (>15%) | Lamination cracks after pressing; low green density; spring-back during ejection | Excessive inlet air temperature causing rapid surface drying and shell inflation | Reduce inlet T by 20–40°C; increase solid content (less water per droplet reduces inflation pressure) |
| Irregular / fragmented granules | Poor die fill uniformity; density variation across tile; inconsistent green strength | Incomplete atomization (viscosity too high or pressure too low); mechanical attrition during pneumatic conveying | Reduce slurry viscosity; increase atomization pressure; inspect conveying system for excessive bends or impact points |
| Excessive fines (>20% below 63 μm) | Die sticking; dust generation; slow die fill (poor flow); air entrapment during pressing | Excessive atomization energy (pressure too high / RPM too high); slurry solid content too low (more fines from small droplets) | Reduce atomization pressure or RPM; increase slurry solid content; consider fine-particle recycling ratio adjustment |
| Excessive coarse fraction (>15% above 400 μm) | Lamination defects; large pores visible on fired surface; density non-uniformity | Worn nozzle orifice (pressure system); insufficient wheel speed (rotary system); high slurry viscosity causing large droplets | Replace nozzle; increase wheel RPM; reduce viscosity via deflocculant |
| Low bulk density (<0.85 g/cm³) | Insufficient green density at standard pressing pressure; need to increase press tonnage | High hollow fraction; angular/fragmented shape preventing close packing; too-narrow PSD | Address hollow fraction root cause; widen PSD; consider rotary atomizer for more spherical granules |
| Sticky / agglomerated granules | Arching in feed hopper; erratic die fill; moisture streaks in green body | Residual moisture too high (>3%); outlet air temperature too low; organic binder migration to granule surface | Increase outlet air temperature; reduce feed rate; verify binder type compatibility with drying temperature |
§5 Integrated Optimization Matrix
Optimizing throughput while maintaining granule quality requires coordinated adjustment across slurry preparation and atomization. The matrix below maps starting conditions to recommended actions:
| Current Situation | Throughput Priority | Granule Quality Priority | Balanced Approach |
|---|---|---|---|
| Low solid content (62–64%) + pressure nozzle | Raise solids +2% via deflocculant optimization; verify atomization quality at elevated solids | If hollow shells appear, reduce inlet T by 20–30°C; maintain pressure at current level to preserve droplet size | Incremental solids increase (+1%) with simultaneous inlet T adjustment; monitor granule PSD weekly |
| Low solid content (62–64%) + rotary atomizer | Raise solids +2–3%; rotary atomizer tolerates higher viscosity better than pressure nozzle | Maintain wheel speed; wider PSD from rotary naturally supports good pressing behavior | Aggressive solids increase (+2%) with wheel speed fine-tuning if PSD shifts too coarse |
| Moderate solid content (65–67%) + any atomizer | Evaluate deflocculant switch from STPP to electrosteric type for +1–3% solids gain | Granule morphology likely acceptable; focus on PSD monitoring during transition | Deflocculant trial at bench scale (1 L slurry) before production trial; verify pressing quality at each +1% step |
| High solids (68%+) but pressing defects | Throughput is already optimized; shift focus to atomization and drying parameters | Investigate hollow fraction (reduce inlet T), PSD width (rotary: adjust RPM; nozzle: stagger orifice sizes), or residual moisture | Hold solids constant; systematically trial one atomization/drying parameter change at a time with pressing feedback |
| Pressing defects but throughput is adequate | Throughput is not the constraint; do not increase solids further | Audit granule PSD, hollow fraction, bulk density, and residual moisture. Each parameter maps to specific pressing defects (see §4.3) | Run diagnostic pressing trial with sieved fractions to isolate whether defect is size-driven or morphology-driven |
§6 Validation & Measurement Protocol
6.1 Slurry Characterization (Pre-Dryer)
Solid Content (Dry Weight Basis)
Weigh slurry sample (~50 g); dry at 110°C to constant weight; calculate: (dry weight / wet weight) × 100%. Measure on each milling batch to establish production run consistency. (ASTM C324 or equivalent moisture content method)
Viscosity Curve (5-Point Dosage)
At target solid content, measure viscosity at current deflocculant dosage and at ±0.05%, ±0.10% from current. Plot viscosity vs. dosage. The minimum identifies the optimum. Verify that minimum viscosity is below the atomization threshold for your dryer (consult dryer manufacturer's maximum recommended feed viscosity).
Rheology Type Check
Measure viscosity at two shear rates (e.g., 10 RPM and 100 RPM on Brookfield). Ratio >1.5 indicates thixotropy (shear-thinning); ratio <0.8 indicates dilatancy (shear-thickening). Near-Newtonian (ratio 0.9–1.2) is preferred for stable atomization.
6.2 Granule Characterization (Post-Dryer)
Particle Size Distribution (Sieve Analysis)
Use a stacked sieve set: 630, 500, 400, 250, 125, 63 μm mesh sizes. Weigh each retained fraction. Calculate cumulative distribution and plot. Measure weekly (or more frequently during process changes) to detect PSD drift. (ASTM C136 / ISO 565 for sieve specifications)
Bulk Density and Tap Density
Free-flow bulk density: pour granules into a graduated cylinder of known volume; weigh. Tap density: tap the cylinder mechanically (or manually ~100 taps) until volume stabilizes. The ratio of tap/free-flow density (Hausner ratio) indicates flowability — values <1.25 indicate good flow. (Adapted from pharmacopoeia and powder metallurgy methods)
Granule Morphology Inspection (SEM/Optical)
Mount granules on adhesive carbon tape. SEM imaging at 30–100× magnification reveals surface texture, sphericity, and hollow shell presence. Cross-section (embed in resin, polish, SEM) quantifies internal porosity. Perform at baseline and after each significant parameter change.
Flowability (Hall Flowmeter)
Measure the time for 50 g of powder to flow through a standardized funnel orifice (2.5 or 5.0 mm). Flow times <30 seconds indicate acceptable pressing feed behavior for most ceramic applications. (Adapted from ASTM B213 for metallic powders; not a formal ceramic standard)
Residual Moisture
Weigh powder sample (~10 g); dry at 110°C for 30 minutes or until constant weight. Target: 0.5–1.5% for tile body powders. Values outside this range indicate outlet air temperature or feed rate adjustment needed.
6.3 Pressing Validation
Green Density
Measure dimensions and weight of pressed green tiles (minimum 5 samples). Calculate density = weight / volume. Compare against baseline. Target standard deviation <0.02 g/cm³ within a sample set.
Green Strength (3-Point Bending)
Cut green test bars (or use tile format specimens). Test in 3-point bending per ASTM C1161 (adapted for green ceramics). Compare against historical baseline. A drop >15% from baseline after a solids increase warrants investigation.
Lamination / Delamination Check
Visual inspection of pressed tile edges and cross-section (cut with a sharp blade). Penetrant dye test: apply a low-viscosity dye to the tile surface; dye penetration into internal cracks flags lamination defects invisible to the naked eye.
§7 Troubleshooting
Spray Dryer Output Lower Than Rated Capacity Despite "Normal" Settings
Excessive Hollow Granules (>15% of population)
Particle Size Distribution Drifting Coarser Over Time (Pressure Nozzle)
Pressing Defects (Lamination) After Solids Increase
Powder Flow Problems (Arching, Rat-Holing in Feed Hopper)
§8 Frequently Asked Questions
Request a Spray Drying Process & Granule Morphology Consultation
Spray dryer throughput and granule quality are tightly coupled engineering problems. Goway's technical team assists ceramic producers in diagnosing the specific interactions between their slurry formulation, deflocculant system, atomization equipment, and pressing requirements — and in developing a coordinated optimization plan that balances output with powder quality.
To submit an inquiry, visit our Ceramic Deflocculant / STPP Replacement product page (/products_detail/6.html) and use the inquiry form. Please include the information below to enable a more targeted response.
Please reference this guide ("Spray Dryer Output Guide") when submitting your inquiry. Providing granule sieve analysis data and SEM images (if available) enables more precise diagnosis of the morphology-throughput relationship in your specific system.
Related Resources
- Spray Drying Energy Optimization — the energy-efficiency complement to this throughput guide; covers deflocculant-driven energy savings framework (visit /News_detail/155.html)
- Reduce Ceramic Slurry Viscosity — deflocculant selection and viscosity reduction methodology for spray drying feed preparation (visit /News_detail/150.html)
- Ball Mill Energy & Grinding Aids — upstream grinding efficiency determines the slurry particle size distribution entering the spray dryer (visit /News_detail/156.html)
- Ceramic Deflocculant / STPP Replacement — Goway FG-2017, FG-MK03, FG-N203B, FG-SL01A product specifications (visit /products_detail/6.html)
Keyword：
More News
Improving Dry Press Strength: How Binders and Lubricants Reduce Cracking and Breakage
2026-06-10
GOWAY INTERNATIONAL MATERIAL CO., LTD
Founded in 2009, we specialize in producing and supplying ,ceramic additives and related products, committing to supplying stable, environmentally friendly,professional and ceramic materials.
Contact UsContact Us
Company Phone/Wechat：86-0757-82131106 / +8613728575572
Company Fax：86-0757-82131106
Whatapp/skype: +8613600032377
E-mail：info6@goway-china.com
Office Address: Room C11-6, Foshan National Torch Innovation and Pioneer Park, Jihua 2nd Road, Chancheng District, Foshan City, Guangdong Province, China.
Factory Address: Nanbian Industrial Zone, Sanshui District, Foshan City Guangdong Province，China.