Dunstable cement logoLogo briefly used by the Dunstable Portland Cement Co. Ltd.


Clinker manufacture operational: 9/1926 - 1971

Approximate clinker production: 11.1 million tonnes (37th)

Raw materials:


The plant was a Maxted & Knott design and was successfully commissioned before the Red Triangle takeover. The plant typified the Red Triangle acquisition policy in that it was superficially up-to-date, although not necessarily technically well-conceived. The plant as originally built was described in an article in The Engineer.

The bizarre shapes of kilns A1-3 arose from a succession of ad hoc modifications. The original kilns had no enlarged sections: Edgar Allen was firmly against these at the time. Desiccators were added to these in the 1930s – the latter could not be added to the end of the kiln because of load considerations, so they were placed before the fourth tyre, and the kilns were truncated. At the same time, the third kiln was added, and precipitators and a common stack were added, the latter being on the centre-line of A2. The third kiln was in the standard Vickers Armstrong format, with enlarged burning zone and desiccator. Subsequently, in a further attempt to increase capacity, A1 and A3 were lengthened with the addition of a further pier, using tube of standard diameter. This was not possible for A2 because of the position of the stack.

Lime had been made by Forders at Sundon, Sewell and Blows Down nearby, and these small plants were replaced by a new plant at Dunstable in 1935, using the Totternhoe Stone intervening between the Chalk Marl and Grey Chalk in the main quarry: there was a block of fifteen kilns by 1938. These were cleared in 1964, making way for the press house for the semi-wet kiln A4 commissioned in 1966. The entirely in-house designed semi-wet project was mis-conceived: the smectite-bearing argillaceous component was unsuitable for pressing, and the Davis preheater had insuperable technical defects. The result was Blue Circle’s shortest-running kiln, with an operating life of less than five years, and a massive capital write-off. Had the plant survived beyond the 1973 energy crisis, the economics of persevering with it might have improved, but the plant had to shut to justify what was increasingly clearly a white elephant at Northfleet. The site remained as a depot for Northfleet cement. The plant used a spur of the Welwyn-Leighton Buzzard railway for transportation: the Dunstable-Luton section continued in operation solely for the plant after the line closed for other traffic in 1965, and remained in operation until the depot closed in 1990. The plant site was cleared and is now covered by an industrial estate, although a few foundations remain around the periphery. The quarries remain un-developed and overgrown.


Washmill systems were established at the various quarries and pumped slurry to the plant.

Four rotary kilns were installed:

Kiln A1

Supplier: Edgar Allen
Operated: 9/1926-08/06/1970
Process: Wet
Location: hot end 501595,223380: cold end 501582,223455: unenclosed.

Rotation (viewed from firing end): initially anticlockwise: from 1948 clockwise.
Slope: 1/24 (2.388°)
Speed: 1.0 rpm
Drive: 45 kW
Kiln profile:

Cooler: Rotary 60’0”× 6’0” (metric 18.29 × 1.829) beneath firing floor
Cooler profile: : 0×1829: 305×1829: 1829×2438: 5791×2438: 7315×1829: 18289×1829: Tyres at 3658, 11430.
Fuel: Coal
Coal Mill: Direct: Initially 112 kW Clarke Chapman pulveriser, with a spare shared with kiln A2. Replaced in 1937 by a Rema roller mill supplemented with Atritor.
Typical Output: 1926-1932 176 t/d: 1932-1947 241 t/d: 1947-1966 297 t/d 1966-1970 286 t/d
Typical Heat Consumption: 1926-1932 9.15 MJ/kg: 1932-1938 8.57 MJ/kg: 1938-1951 8.10 MJ/kg: 1951-1966 8.37 MJ/kg: 1966-1970 9.12 MJ/kg

Kiln A2

Supplier: Edgar Allen
Operated: 9/1926-08/06/1970
Process: Wet
Location: hot end 501604,223382: cold end 501594,223438: unenclosed.

Rotation (viewed from firing end): clockwise.
Slope: 1/24 (2.388°)
Speed: 1.0 rpm
Drive: 45 kW
Kiln profile:

Cooler: Rotary 60’0”× 6’0” (metric 18.29 × 1.829) beneath firing floor
Cooler profile: 0×1829: 305×1829: 1829×2438: 5791×2438: 7315×1829: 18289×1829: Tyres at 3658, 11430.
Fuel: Coal
Coal Mill: as kiln A1.
Typical Output: 1926-1932 202 t/d: 1932-1942 294 t/d: 1942-1951 270 t/d: 1951-1958 278 t/d: 1958-1966 293 t/d: 1966-1970 252 t/d
Typical Heat Consumption: 1926-1932 8.86 MJ/kg: 1932-1951 8.22 MJ/kg: 1951-1966 8.82 MJ/kg: 1966-1970 9.36 MJ/kg

Kiln A3

Supplier: Vickers Armstrong
Operated: 1937-08/06/1970
Process: Wet
Location: hot end 501613,223383: cold end 501600,223457: unenclosed.

Rotation (viewed from firing end): clockwise
Slope: 1/24 (2.388°)
Speed: 1.0 rpm
Drive: 45 kW
Kiln profile:

Cooler: Rotary 59’10”× 6’4” (metric 18.24 × 1.930) beneath firing floor
Cooler profile: 0×1930: 152×1930: 1118×2330: 5080×2330: 6045×1930: 18237×1930: Tyres at 3810, 14630.
Fuel: Coal
Coal Mill: Direct: Rema roller mill supplemented with Atritor
Typical Output: 1937-1948 264 t/d: 1948-1952 283 t/d: 1952-1956 306 t/d: 1956-1959 266 t/d: 1959-1966 302 t/d: 1966-1970 268 t/d
Typical Heat Consumption: 1937-1952 8.20 MJ/kg: 1952-1956 8.41 MJ/kg: 1956-1959 8.13 MJ/kg: 1959-1966 8.50 MJ/kg: 1966-1970 9.10 MJ/kg

Kiln A4

Supplier: Vickers Armstrong
Operated: 15/08/1966-31/3/1971
Process: Semi-wet: Davis Preheater
Location: hot end 501625,223383: cold end 501615,223443: entirely enclosed.
Dimensions: 200’0”×14’0”BC / 15’0”D (metric 60.96 × 4.267 / 4.572)
Rotation (viewed from firing end): ?
Slope: ?°
Speed: ?
Drive: ?
Kiln profile: 0×3658: 737×3658: 2743×4267: 47396×4267: 51816×4572: 60960×4572: Tyres at 4572, 26822, 52730
Cooler: Fuller 850H grate
Fuel: Coal
Coal Mill: Direct: MPS100 roller mill
Typical Output: 894 t/d
Typical Heat Consumption: 4.82 MJ/kg

Sources: Cook, pp 72, 75: Jackson, pp 223, 278: Pugh, pp 109, 154-155, 263: “The Dunstable Portland cement works”, The Engineer, CXLV, January 27, 1928, pp 92-94, 104; February 3, 1928, pp 120-123 - read this article.

Read The Engineer at Grace's Guide.

The Dunstable Portland Cement Company Ltd was formed in February 1925 and opened its plant during 1926 only 4.6 km from Sundon, then well-known to be Britain's lowest-cost plant, and using essentially the same raw materials. Shortly after commissioning, The Engineer (CXLV, January 27, 1928, pp 92-94, 104; February 3, 1928, pp 120-123), published an in-depth account of the plant. It is believed to be out of copyright. Although not mentioned in the article, the machinations associated with the formation of Red Triangle were under way at the time, and perhaps for this reason, the article was more than usually fulsome. Becoming, by 1931, part of the Blue Circle Group, the plant continued in operation until 1971, never achieving the low-cost status to which it aspired.

The text has been transcribed from the original article. The figures have been presented in the order referenced in the text rather than numerical order.

Values of imperial units (as of 1928) used in the text (alphabetical order): 1 acre = 0.40468424 Ha: 1 ft = 0.30479947 m: 1 gallon = 4.5460756 dm3: 1 HP (horse-power) = 0.7456998 kW: 1 inch = 25.399956 mm: 1 psi (pound-force per square inch) = 6.89478 kPa: 1 ton = 1.01604684 tonne: 1 yard = 0.91439841 m.

The Dunstable Portland Cement Works.

By courtesy of the Dunstable Portland Cement Company, Ltd., we have recently had opportunities of making thorough inspections of the new works which have been established by it just outside the town of Dunstable in Bedfordshire. That part of the country is strongly undulating, and is particularly interesting in that the three chalk strata—upper, middle and lower—outcrop at the surface at points which are in some cases close to one another. On the land on which the works have been built there are, but a short distance apart, outcrops of the middle and lower chalk (Note 1), and their chemical compositions are such that when mingled together in the correct proportions, the mixture contains, without any further additions, the exact ingredients required for the manufacture of Portland cement of high quality (Note 2). Both chalks are easy to work, for both can be dealt with in wash mills after being passed through kibbling rolls to break up the lumps as quarried, and neither contains any flints, the occurrence of flints being confined to the upper chalk. There is moreover, but little overburden. In some cases the chalk comes practically to the surface; in others, it is only covered by a few inches of soil; and nowhere does the depth greatly exceed 18 in. The site therefore may be looked upon as being ideal from the point of view of raw materials, and the company owns some 600 acres, with usable material going down for perhaps hundreds of feet before the greensand which underlies it is reached (Note 3).

Fig 1
Figure 1: Diagrammatic plan of Dunstable Portland cement works

In addition to their advantage regarding raw materials, however, the works are situated on a main road (Note 4), from which there is easy access to many towns, large and small, within economic carrying distance by motor lorry, those towns including Bedford, Luton, &c., all of them rapidly growing and likely to need large quantities of Portland cement, while London is also within easy road delivery. Furthermore, the site is in direct connection by the line marked D in Fig. 2 with the London, Midland and Scottish, and the London and North-Eastern railway systems (Note 5), so that coal and gypsum are readily brought to it, and cement, as readily, sent away. At the moment, the company has not got them, but it intends shortly to order a fleet of 20-ton bottom-discharging railway wagons, which will bring coal from various collieries in the Midlands—none of them at prohibitive distances away—empty their contents into a hopper, and then be hauled back to fetch further loads. In this connection it may be explained that extensive sidings have been provided—see E in Fig. 2—for the temporary use of loaded or empty wagons, and that the company has, for shunting purposes, an exceedingly handy standard-gauge locomotive made by the Sentinel Waggon Works, Shrewsbury.

Fig 2
Figure 2. Birdseye view of works

As a final advantage, it may be said that during a large portion of the year there is a superabundance of water draining from the site to a sump, from which what is not required for the time being is pumped into a reservoir, which has a capacity of 100,000 gallons, and commands one set of wash mills. Arrangements have also been made by which, during the drier months of the year, the effluent from a nearby works (Note 6) may be drawn upon. So that from every point of view it is hard to imagine a better position in which to found a cement factory to operate on the "wet" system, which has been chosen by the consulting engineers, Messrs. Maxted and Knott (Note 7), of 82, Victoria-street, S.W., by whom the works have been designed. Furthermore, it may said at the outset that the works have been laid out in a thoroughly practical and apparently most economical manner, and that the whole of the machinery, the chief contractors for which were Edgar Allen and Co., Ltd., of Sheffield, is of the highest class.

The respective chemical compositions of the two kinds of chalk were, at the time of our visits, such that approximately two-thirds of the middle chalk and one-third of the lower chalk were required to produce the correct mixture for the manufacture of Portland cement. For convenience in describing the plant and processes, we shall use the terms "chalk" and " clay", as is commonly done in the works, to describe the two materials, though "clay" is not actually a correct description to apply to the marl-like lower chalk (Note 8). It may be possibly found in time when the excavations of the two strata have proceeded far enough for the dividing line or zone between the two strata to be reached, that the material as excavated will, without any admixture or adjustment, have the correct composition for cement making, but at present, as we have said. approximately two parts of chalk are required to one part of clay. Consequently, we find, as might be expected, that the plant for dealing with the clay is of just half the capacity of that for dealing with the chalk. Both the clay and the chalk are led to the works in pipes in the form of slurry, being mixed in the desired proportions at a point some 270 yards away, as will be explained in due course. Our description will be more readily understood by the aid of the accompanying plan and of Fig. 2, which is reproduced from a bird's-eye photograph taken from an aeroplane.

The clay is at present being quarried at a point some 800 yards to the left of the point marked A in Fig. 2 (Note 9), and at an elevation of some 150 ft. below it. The clay is being got out by a steam-operated Ruston caterpillar digger, having a bucket with a capacity of just over a ton. It is delivered direct into a train of four side-tipping steel trolley wagons which run on 2ft.-gauge lines laid on the floor of the quarry. For the most part the material is soft and homogeneous and consistent in chemical composition, though very occasionally shallow bands of much harder stuff are encountered. The chemical composition of these harder bands is almost identical with that of the surrounding material, but as the blocks into which they are broken by the digger are hard enough to put too severe a stress on the kibbling rolls, which were, as a fact, not designed to deal with them, they are removed by hand before the material is shot into the wash mill. The quantity of these hard lumps is not very large, however, the pile representing some nine or ten months' working of the plant, not being of inconvenient proportions.

Fig. 3
Figure 3: Plan and sections of marl quarry plant

Two trains of light trolley wagons are at present being operated. When one train is full it is hauled by a small petrol locomotive from the quarry to the wash mill, a distance at the moment of some couple of hundred yards. Having done the journey with loaded trucks, the locomotive picks up the train of empty trucks and hauls it back to the quarry, sidings being arranged in the lines of railway to render these operations possible. Arrived at the wash mill, the loaded trucks are tipped one by one and their contents shot into a hopper over the kibbling rolls—Fig. 3. These rolls are actually two sets of fingers curved to sickle form and mounted on two parallel horizontal shafts. The fingers on the two shafts interlace with each other, and the two shafts revolve at different speeds, one making 1.9 revolutions a minute and the other 0.95. The machine works exceedingly well (Note 10), the material being broken up into pieces of such sizes that they are readily dealt with in the wash mill. With regard to the latter, nothing much need be said, saving that it is 20 ft. in diameter and that its arms are revolved at a speed of 20 revolutions per minute, by means of a three-phase alternating current electric motor of 100 horse-power. The slurry discharged from the wash mill is forced by a three-ram plunger pump through 720 yards of 5 in. piping to a concrete storage tank built near the point A in Fig. 2, the difference in level being about 120 ft. It was at first intended that both the wash mill and the pump should be operated by the same motor, but it was discovered, when operations were started, that the "clay" formed a slurry of such a "stiff" consistency that one motor would be overloaded if it drove both mill and pump, and, accordingly, an additional motor was installed to drive the latter. The viscosity of the slurry is, in fact, much greater than is ordinarily experienced with slurries made from chalk marls in other parts of the country, and it made itself felt in other parts of the works as well as in the clay pumping plant (Note 11).

Fig. 7
Figure 7: View towards the washmills from the chalk quarry, with the main plant behind.

The chalk is dealt with in the buildings at the point A in Fig. 2. At the present moment the working face in the chalk quarry is about 200 to 300 yards away to the left (Note 12), and the two points are linked together by exceptionally well laid standard-gauge lines of rails, Fig. 7. The overburden is being removed by means of a handy little caterpillar runabout tractor, which hauls a set of three-scraper soil removers termed Baker Maney scrapers, and was supplied by Tractor Traders, Ltd., Smith's-square, Westminster. The equipment is worked by two men—a driver and a man to operate the scrapers. On arriving at the point from which it is desired to remove overburden, the scraper operator first of all releases a catch holding the leading scraper free of the ground, so that the latter revolves on trunnions till its cutting edge engages with the surface of the ground and penetrates below the latter to a fixed amount. As the scraper is dragged forward, its container rapidly fills, when the cutting edge is automatically lifted from the ground. The operator then puts the second scraper to work, and subsequently the third. The train then proceeds to a dumping place where the material removed is automatically discharged, and goes back again to continue operations. The overburden is neatly and cleanly removed by this method, and we are assured that the cost of doing the work is remarkably low. In some parts it is only necessary for the ground to be traversed once, since, as we have explained above, the overburden is, in places, very shallow. In other parts, however, it is necessary to go over the ground more often, but taking all that into account, the cost of removal compares most favourably with that of any other method.

Fig. 6
Figure 6: Ruston steam excavator at the chalk face. The remains of the Houghton Regis windmill is rear right.

The chalk is quarried by means of a Ruston steam caterpillar digger, Fig. 6, page 104, which has a capacity of about 2 tons per stroke. The material, which is greyish white on being first exposed, and is of a fairly hard nature, is dumped direct into a train of two drop-sided tipping railway trucks, and taken direct to the chalk slurry works, by means of a petrol-driven locomotive made by the Motor Rail and Tramcar Company, of Bedford. Arrived there, the contents of each truck are discharged into one or other of the hoppers over two sets of kibbling rolls, of a type identical with that at the clay mill. Beneath each set of rolls is a wash mill of the ordinary type, 20ft. in diameter, the spider of which is, in each case, revolved at 20 revolutions per minute by means of a 100 horse-power alternating-current motor. While the chalk is being washed down, clay slurry, in the proportion arranged by the works chemist, is allowed to flow by gravity from the storage tank, referred to above, into the mills where it becomes thoroughly mixed with the chalk to form a thick slurry of a dark cream colour. The chalk plant is shown in Fig. 4.

Fig. 4
Figure 4: Plan and Sections of Chalk Plant. View in higher definition.
Dunstable cement works slurry screeners
Figure 8: Set of screening mills (9 in total) for sieving the slurry, returning unground material to the washmills

The discharge from the wash mills flows through screens in the ordinary way into a common sump into which dip the buckets of a slurry lifting wheel 28ft. in diameter (Note 13), which is revolved at a speed of 5 revolutions per minute. The buckets of the wheel discharge the slurry at the top into a wooden trough through which it flows into a header leading to a battery of nine slurry separators, Fig. 8, which are operated by belt from shafting which, in turn, is driven by two 50 horse-power motors, one at each end, and from which the lifting wheel is also driven. Drawings of one of the separators are given in Fig. 5 (Note 14). The machine comprises a vertical spindle driven by bevel gearing from a countershaft. Keyed to the vertical spindle is a hollow spider, through which the slurry is fed, and bolted to the spider is a horizontal beater plate carrying cast steel beater brackets and spring steel beaters. This portion revolves inside a cast iron casing, and by centrifugal force throws the slurry on to a series of sieves round the periphery of the casing. The fine slurry is forced through these sieves and flows round the annular trough outside the casing through two outlets for the finished slurry. The tailings or rejects from the screen flow out through a special opening in the casing, and are returned to the wash mill for further grinding. The direction of the rotation of the beaters is shown on the plan, and the speed of the machine is 140 revolutions per minute.

Fig. 5
Figure 5: Slurry separator. View in higher definition.

The discharge from these separators is into a wooden trough from which any one of three mechanical mixers which are arranged to form three arms of a cross—may be fed. The mixers are tanks, sunk in the chalk and lined with brickwork (Note 15). Each is 62ft. long and 30ft. wide, with rounded ends. Each was originally furnished with a set of three mechanical stirrers, each set being slowly revolved by means of 20 H.P. motors through gearing. As a matter of fact the centre of the three stirrers has now been removed from each of the mixing tanks, for the consistency of the slurry, to which we have already referred, was so thick and viscous that it was found that the motors were rather overloaded when three stirrers were at work, notwithstanding the fact that the same size of motor is operating precisely similar mixers in other parts of the country with slurries of ordinary consistency. Moreover, it was found that two sets of stirrers kept the slurry amply agitated (Note 16), there being no tendency for the more solid particles to settle to the bottom. We may here mention that the slurry in the mixers, and indeed as it is supplied to the kilns, contains about 40 per cent. of moisture (Note 17). We may also explain that samples of the contents of these tanks are frequently taken by the works chemists and analysed, any necessary alteration in the proportions of chalk and clay being then made by the attendants adding more of one or the other—as the case may require—to the contents of the wash mills. As a matter of fact, however, as far as our observations went on the occasions of our visits to the works, it is very rarely indeed that any change in the proportions is required. In spite of the fact that the men in charge of the wash mills are dealing with such varying quantities as truck loads made up of discharges of the contents of the buckets of mechanical diggers—which may or may not be all of the same weight, and may not always arrive at the point of discharge at absolutely the same intervals—they get, in time, to be extraordinarily expert in so apportioning the ingredients that a slurry of consistently even composition is obtained. We have noticed the same thing in many cement works, and when it is considered within what comparatively narrow limits variation of the constituent ingredients in Portland cement is permissible, the skill acquired by these men is all the more remarkable. It would almost seem that they almost know by the look of the slurry whether it is "right" or "wrong" (Note 18).

Fig. 9
Figure 9: Edgar Allen 3-throw pump for transfer of slurry from the quarry washmills to the kiln-feed storage tanks. The slurry separators are in the background.

The contents of the mixers can be discharged into a sump formed where the three ends of the mixers converge together. From the sump the slurry is pumped by a three-throw plunger pump having rams 10¾ in. diam. and 15 in. stroke, Fig. 9, to the cement works proper through some 270 yards of 6 in. steel piping. The pump is driven by a 20 H.P. motor. The piping is laid under ground, and where it passes under the roadway seen in Fig. 2 it is taken in one of two 12 in. diameter earthenware pipes laid in concrete. The slurry is discharged into either one of two storage silos—see B in Fig. 2—which are circular vertical riveted steel tanks, 24ft. diameter by 53 ft. 9 in. total height, with funnel-shaped bottoms (Note 19). The two silos contain enough slurry for thirty hours' operation of the kilns. In these silos the slurry is kept agitated by means of compressed air, for which purpose a three-cylinder Broom and Wade air compressor, driven by a 50 H.P. motor through gearing, has been installed. The air is delivered at the bottoms of the silos at a pressure of about 25 lb. per square inch through special agitation nozzles and valves by means of which it is possible to turn on or cut off and control the supply at will. The air thus supplied under pressure rises to the surface of the slurry in great bubbles, which cause sufficient agitation to keep the slimy mass thoroughly mixed.

In a house near the bases of these silos there are, in addition to the air compressor, two sets of three-throw plunger pumps with rams 8⅝ in. in diameter by 16 in. stroke, driven by a 20 H.P. motor. Ordinarily only one of these pumps is in operation, the other being kept as a stand-by. It lifts the slurry from a sump into which it can flow by gravity from either of the two silos, or into which if need be the slurry coming from the mixing plant can be discharged direct, and delivers it into two measuring tanks, arranged immediately above the charging ends of the two kilns. The pumps are capable of lifting considerably more slurry than is actually required for feeding the kilns, and considerably more than that amount is continuously pumped, the surplus, after flowing over a weir in each measuring tank, which gives a fixed head in the latter, being returned in a constant stream to the storage silos, a process which assists in keeping a good average mixture of the chemical constituents of the raw material.

The desired quantity of slurry is fed into the kilns by allowing the slurry to flow through an orifice of prescribed cross-sectional area under the influence of an accurately maintained pre-determined head (Note 20). There are, of course, other methods of arriving at the same result, several of which we have described in the past. but that which is employed at Dunstable is very simple, is perfectly satisfactory, and, moreover, can be relied upon to operate with a minimum of supervision. As long as the flow of slurry is maintained considerably in excess of the requirements of the kilns, practically all the attention that is required is to make sure from time to time that the chute from the measuring tank to the kiln is kept clear. Alteration of the output of the kilns can be effected by varying the area of the orifice. Experiments have been made with the Rigby-Allen slurry-atomising process, by means of which the slurry is forced under pressure through nozzles into the kilns instead of being delivered in the manner described above. Although we understand that the experiments with this plant have been promising so far as they have gone, pointing to an increased output from the kilns and a more economical use of fuel, the apparatus was not working when we visited the works, but we understand that it will be in operation in the near future (Note 21).

Fig. 10
Fig. 10: Longitudinal Section, Elevation and Plan of Dunstable Cement Works. View in higher definition.

Above we had got as far in our description of the Dunstable Portland Cement Works as the slurry silos, and the method of feeding the slurry into the kilns. There are, as was intimated, two kilns—C, Fig. 1 ante. They are, of course, of the rotary type, and each is 200 ft. long by 9 ft. 8½ in. diameter throughout, there being no enlargement in diameter in the firing zone. It may be remarked in passing that, though, when they were first introduced, great things were claimed for the kilns with enlarged portions for the firing zones, those claims would seem not to have been substantiated, since of recent years many parallel kilns have been installed (Note 22).

Fig. 13
Figure 13: The Kilns from the Firing Platform - No 1 to the left.
Fig. 14
Figure 14: The Kilns from the Feeding End - No 1 to the right.

There is nothing particularly novel in the construction of the kilns to which to draw special attention. They are given an inclination of 1 in 24, and are carried in the ordinary way on four cast steel tires, 16 in. wide, one near each end with the others spaced at regular intervals, which each bear on large rolling wheels free to revolve, the lower portions of which dip into oil and water troughs. At the time of our last visit, each kiln was revolving about once every 95 seconds, and we were informed that the output of each was upwards of 1000 tons of clinker per week (Note 23). The driving gears are of cast steel throughout, and all the wheels are machine cut, with the exception of the large spur ring which embraces the kiln and the pinion which gears with it, both the latter being machine moulded. Each kiln is driven by belt from a 60-30 H.P. induction motor capable of a speed variation of from 725 to 560 revolutions per minute, the variation being effected from the firing platform by the man in charge of the kilns (Note 24).

The firing hoods of the kilns are of Messrs. Edgar Allen's standard type and do not call for any special comment. They are, as usual, furnished with wheels running on rails, by means of which they can be withdrawn from the ends of the kilns. Powdered coal is used for fuel, and the powdering of the coal is effected in three turbo-pulverisers made by Clarke, Chapman and Co., Ltd., each of which is driven direct by a 150 H.P. motor running at 1470 revolutions per minute—see Fig. 15 (Note 25). One pulveriser is arranged opposite the end of each kiln, and the third unit is placed midway between the first two, and the delivery piping and valves are such that the third or central pulveriser, which ordinarily remains as a standby, may be used to feed either of the kilns. Hot air from the coolers is supplied to the pulverisers and the air suction ducts leading to the kilns are also connected to the cooler hoods. When the works were first put into operation, the pulverisers were fed with raw coal taken direct from the storage heap, and we are informed that, during the coal dispute of last year, the coal, as delivered, sometimes contained as much as 20 per cent. of moisture, but that the pulverisers despite these difficult conditions continued to work without interruption. However, a coal dryer has since been installed (Note 26). The coal used for firing the kilns is brought on to the site in railway wagons, the wagons being shunted so as to come over a grating above a large underground hopper into which dips a continuous bucket conveyor. The latter lifts the fuel, which is in the form of small slack, to a floor arranged above three large riveted steel hoppers, one of which is over each of the three pulverisers on the kiln-firing floor. Each of these hoppers contains 75 tons of coal, and the discharge from the elevator is into a swing tray conveyor, which delivers it at will into either of the three hoppers, or, alternatively, transport it along to the far end of the building, where it may be taken in hand by a further conveyor and discharged into a hopper, capable of containing 100 tons, arranged above the coal-drying building. The coal dryer, which, as explained earlier, is a comparatively recent addition, is of the Edgar Allen Class 8, double-shell type. It is 5 ft. in diameter and 30 ft. long, and has a coal-fired furnace with double doors. The coal to be dried is fed into the drum from a revolving table, the delivery being into a screw conveyor and thence by means of bucket elevators to the hoppers above the kiln floor, into which it is delivered by means of a spiral conveyor.

Fig. 11
Fig. 11: Section through Coal Handling and Drying Plants.
Fig. 15
Fig. 15: Coal Pulverisers on Firing Platform. Clarke Chapman Turbo-pulverisers - No 1 to the right and the common spare to the left.

The hot clinker from each kiln is discharged into a cooler 6 ft. in diameter and 60 ft. long, the coolers being arranged in a direct line with the kilns (Note 27). The clinker therefore as it comes from the kilns is taken on in a straight line towards the grinding mills, and not, as is done in some cement works, led back under the kiln in order to save space. The coolers are of quite ordinary construction, and each is driven at a constant speed by a 10 H.P. motor. At the discharge end of each cooler is a measuring device—Fig. 17—which is furnished with a counter, so that the volume of clinker produced is recorded (Note 28). The discharge from both coolers is into a horizontal swing tray conveyor (Note 29), which is controlled by an air dashpot, and which, in its turn, delivers the clinker into the boot of a continuous bucket elevator. The latter raises the clinker to the top of an adjoining building, the upper part of which forms a large storage silo (Note 30), while the grinding machinery is at the ground level. At the top of the building there is a horizontal swing tray conveyor of the same type as that just referred to as receiving the discharge from the coolers, by means of which the clinker is delivered into the silo below or taken on to the far end of the building, where it may be discharged down a shoot into a hopper erected on a wooden staging outside the building, with its floor some 20 ft. from the ground. On this staging, which is furnished with a weighing machine, run narrow-gauge lines of railway along which trolleys. after receiving a weighed charge of clinker from the hopper, can be run on to outside storage heaps and discharged. The elevator and conveyor in this building are both driven by one 20 H.P. motor, arranged on the top floor. A section through the grinding building is given in Fig. 19.

Fig. 19
Fig. 19: Section through Clinker Grinding Department.
Fig. 17
Fig. 17: Clinker Measuring Device at Discharge End of Cooler.

The grinding machinery consists of two Edgar Allen combination tube mills, each 7 ft. in diameter and 36 ft. long. This type of mill—Fig. 16—has already been described in our columns and need not here be referred to in detail. Each is driven through single-reduction double-helical machine-cut cast steel gear, which is contained in special dust-proof casings. The pinion countershafts are each connected. through flexible couplings, with the shaft of a 550 horse-power motor. We shall refer to these motors again later. The clinker, which is led down chutes from the silos above, is supplied to the tube mills by means of an adjustable table feed in the usual way, a slight sprinkle of water being sprayed on to the tray conveyor. The necessary quantity of gypsum is added mechanically to the clinker at the inlets to the mills.

Fig. 16
Fig. 16: Combination cement-grinding Tube Mills. No 1 to the left.

The finished cement as it comes from the mills is delivered into a spiral conveyor, which takes it out of the clinker building to the cement storage silos. The latter, of which there are four, arranged close together so as to occupy the four corners of a square, are of riveted steel plate. 30 ft. 6in. in diameter by 50 ft. high. Each silo holds 1500 tons, so that the total storage available is 6000 tons (Note 31). The delivery from the spiral conveyor is into the boot of a totally enclosed bucket elevator, which raises the cement to a covered-in floor formed above the tops of the silos, the discharge being into further spiral conveyors which deliver the cement into either of the four silos at will. Below the silos are two tunnels in which valve-controlled chutes lead down to spiral conveyors, one on each side of each tunnel, so that cement can be drawn from any desired silo. The conveyors take the cement to an elevator, which lifts it and discharges it into a further conveyor, which, finally, delivers it into hoppers arranged in the upper part of the dispatch shed. The latter is a roomy building which has on each side of its loading platform a standard gauge siding, so that railway wagons can be loaded direct. On the loading platform, in addition to ten valve-controlled spouts for filling sacks by hand, there are two Bates' valve bag packers—Fig. 18—each capable of packing 25 tons of cement per hour into sacks, the sack mouths being closed by a twisted wire. As each sack is filled, it is run down a slide on to a hand barrow, on which it is first run to a weighing machine and then taken direct into a railway van drawn up to the platform for the purpose, or to another part of the loading platform, where it can be loaded on to carts or lorries for dispatch by road.

Fig. 12
Fig. 12: Cement Storage Silos and Packing House.
Fig. 18
Fig. 18: Bates Valve-bag Cement Packers.

Reverting now to the kilns, it may be explained that the hot gases, after passing through the kilns, are drawn downwards by means of two induced draught fans—one for each kiln—through spacious baffled depositing chambers where a very large proportion (Note 32) of the dust in suspension is thrown down. This dust, if it were not removed in this manner, would not only cause a nuisance in the neighbourhood by covering the vegetation, &c., in the surrounding country after being taken up by the draught and discharged from the chimney, but it would also represent a very considerable loss, since it consists almost entirely of partially burnt slurry. Arrangements have therefore been made by which the dust deposited in the flue chambers is withdrawn by spiral conveyors and led to a sump formed below the floor of the building which contains the pumps that feed slurry to the kilns. In that sump there is a revolving stirrer by means of which the dust is mixed with the slurry delivered from the slurry silos and is again fed into the kilns (Note 33). The induced draught fans were made by Davidson and Co., Ltd., of Belfast, and each is driven by a 40 H.P. variable-speed motor running at 362 revolutions per minute maximum. They both discharge into a single brick chimney, which is 11 ft. 9 in. in internal diameter and 170 ft. high.

While on this subject of dust, we may explain that throughout the works there are, in every department where dust is formed, elaborate arrangements to prevent the spread of dust, and, incidentally, to save money in the process. Each building is furnished with one or more dust-collecting devices, made by A. and B. Harris, Ltd., of 47, Victoria-street, Westminster, S.W.1, and each device has its collecting sack or other receptacle, into which the dust is delivered and saved for further use. In this way the waste of many hundreds of pounds worth of material is prevented in the course of a year, and all the departments are kept remarkably free from dust and dirt. In the case of the clinker grinding room, the dust collected is actually delivered from the collector into the finished cement spiral conveyor, and is taken away to the storage silos. This step is, of course, quite permissible since the dust is practically pure Portland cement, and it is of such great fineness that it would all of it, probably, pass through a 180 by 180 sieve.

The whole of the works is operated electrically, the necessary energy being obtained from the mains of the Luton Corporation, the distance transmitted being about 3 miles (Note 34). Three-phase 50-period current is delivered at 6600 volts pressure to transformers—supplied by the Hackbridge Electric Construction Company, Ltd., of Hersham, Surrey—contained in a specially built brick sub-station erected on the works site. The transformers are of 760 kW capacity, and there are two of them. In all, there are as many as sixty-three motors installed throughout the works, and they vary in capacity from 5 to 550 horse-power. For all of them, except two, the 6600-volt pressure is stepped down to 415 volts, and all, again except two, are induction machines. The exceptions are the two 550 horse-power machines which drive the clinker grinding mills. These machines, we may explain, are in a room separated from the mill room by a wall through which the driving shaft passes, so that they are entirely cut off from the grinding machinery. They are of the asynchronous-synchronous type, and they operate directly off the 6600 V mains. All the motors were supplied by the English Electric Company, Ltd., and were manufactured at the Phoenix Works, Bradford.

One of the great businesses of a large cement works is the maintenance of the sacks, in which the material is dispatched, in good condition. Sacks are returned in large it from consumers, and, generally speaking, they are in a very dirty and muddy condition when they arrive, besides being, more often than not, soaking wet and frequently torn. The Dunstable works are particularly well equipped for dealing with this question. There are specially arranged drying rooms, beating machinery, &c., by means of which the sacks are thoroughly dried and cleansed. Each sack is then carefully examined and any necessary repairs effected. Then, too, there is a battery of power-operated sewing machines for sack repairs. How big this sack problem is may be understood since it is known that as many as 1,200,000 sacks are filled and dispatched from the works in the course of a year.

It is important in a cement works, too, that there should be facilities for readily and rapidly carrying out any repairs that may become necessary. In this particular, the Dunstable works are also well off, for there are both fitting and joiners' shops which contain all the tools for wood and metal working which are likely to be required. It is noteworthy, however, so we gather that, in spite of the fact that the works have been in operation for twelve months and more, there has never yet been a really serious breakdown, which speaks well, not only for the material supplied by the contractors, but also for the care with which it has been looked after and maintained.

What may certainly be accounted among the most important parts of a cement works are the chemical and physical laboratories, and in this direction the works have been specially well provided. The laboratories, which are housed in one of the administration buildings, shown at F in Fig 1 ante, are bright rooms, well found in every way. In them, analyses and tests are being continually carried out, and it can be said of the investigators that they have the satisfaction of being able to show that the cement produced in the works is of an exceedingly good quality. In this connection we are able to reproduce below some independent tests made, after manufacturing operations had only been in progress for a few months, by Messrs. Henry Faija and Co., of Westminster:—

Results of Tests of Dunstable Portland Cement made by Henry Faija and Co.


Residue when sifted through a 180 x 180 sieve 2.0%
Residue when sifted through a 76 x 76 sieve Nil

(British standard specification requirements—10% maximum and 1% maximum respectively).

Tensile Strength per Square Inch.

Water used for gauging, 20%; briquettes placed in water twenty-four hours after gauging; strain applied at the rate of 100 lb. in 12 sec. in a standard testing machine.

Neat Cement: Seven Days' Test.

No. 1 broke at940 lb.
No. 2980 lb.
No. 3920 lb.
No. 4945 lb.
No. 5930 lb.
No. 6985 lb.
Average950 lb.

(British standard specification requirements-600 lb.).

Tensile strength per Square Inch ; Sand Test.

Three parts standard sand to one part cement, gauged with 7.5% water. The briquettes were placed in water in twenty-four hours from gauging, where they remained until due for testing, when they were broken in a standard testing machine with the following results:—

Age, dayslb. per square inch
123456Ave.MPa (Note 35)
Two-days' test. 2902702753302953403007
Three-days' test. 56059054058556059057119
Four-days' test. 62059559058557059059221
Five-days' test. 58064061061563064562025
Six-days' test. 62563066064565063064029
Seven-days' test. 66567565067066071067232

(British standard specification requirements—Seven days, 325 lb.).

Crushing Strength per Square Inch.

Cubes of neat cement, and also composed of three parts of standard sand to one of cement by weight, gauged and treated in an exactly similar manner to the above briquettes, were tested for crushing strength, with the following results:—

Seven days' Test: Neat Cement.

No. 1 crushed at9147 lb.
No. 29499 lb.
No. 39147 lb.
No. 49850 lb.
No. 59499 lb.
No. 69324 lb.
Average9411 lb.

Three Parts Standard Sand to One Part Cement.

No. 1 crushed at5265 lb.
No. 25083 lb.
No. 35446 lb.
No. 45265 lb.
No. 55083 lb.
No. 65355 lb.
Average5249 lb.

Setting properties:—

Initial 1½ hours
Final 3 hours

Soundness—Le Chatelier. Sample expanded 1 mm. after twenty-four hours' aeration.

(British Standard specification requirements—Expansion not to exceed 10 mm.)

As will be observed, these are exceptionally good results. We understand that, latterly, the company has been turning out a rapid-hardening cement, to which it has given the name of "Rapard" (Note 36), and that it has been quite as successful, in its own special way, as the ordinary Portland cement.

In conclusion, we desire to tender our best thanks to the company for facilities for visiting the works; to Mr. C. B. Leonard, the works manager, and Mr. Wilson, the chief engineer, for courteous help during our visits; to Messrs. Maxted and Knott for valuable assistance during the preparation of this article; as well as for some of the illustrations which accompany it; and to Edgar Allen and Co., Ltd., for supplying particulars of the plant and equipment.


Note 1. Here and throughout the article, the writers are presumably relying on the site staff's understanding of the geology they were working, which was clearly slight. The quarries contained only Lower Chalk. See discussion of geology below.

Note 2. The exact composition of good cement is open to debate. Dunstable's chemistry was in fact fairly eccentric, due to the high silica ratio of the material.

Note 3. Of course, all the material is "useable", but the majority of the material is low in calcium carbonate, and is only useable if there is sufficient high-carbonate material to go with it. See geology. The excavation didn't go anywhere near the base of the marl.

Note 4. The A5 was regarded as a major arterial road at the time.

Note 5. The LMS line connected Dunstable North with the Euston-Birmingham line at Leighton Buzzard. The LNER line ran through Dunstable Town and Luton to join the King's Cross-York line at Welwyn. Most cement freight went via the latter to London. The Luton-Dunstable section remained open solely for cement traffic after the Welwyn-Leighton Buzzard line was closed for all other purposes under the Beeching Act in 1965.

Note 6. The Dunstable Municipal Sewage works was at the foot of the hill, about 500 m from the marl pit's washmill. Many cement plants used sewage effluent for making slurry, and this obviated the need to make the effluent of drinkable standard.

Note 7. G. V. Maxted was also a Director of DPCC Ltd. The others were Godfrey Butler Hunter Fell (chairman), Alfred Brice Cockland (MD), James Felix Cunningham, the Earl of Dunmore and Percy John Neate.

Note 8. The geology of the reserve (and presumably also its extent) were not understood. The Lower Chalk (the Cenomanian) in the area is divided into two roughly equal layers - the Gray Chalk (Zig-zag Chalk Formation) above and the Chalk Marl (West Melbury Marly Chalk Formation) below - with the prominent Tottenhoe Stone marking the boundary. When the writers here say "Middle Chalk", they mean Gray Chalk, and by "Lower Chalk", they mean Chalk Marl. See discussion of geology below. Terming the Gray Chalk "chalk" and the Chalk Marl "clay" was also practiced at Sundon, Arlesey and Barrington, and one must be aware of this when reading accounts of these plants. The chalk marl contained calcium carbonate in the range 60-75%, so it could not by any stretch of the imagination be called a clay.

Note 9. Located at B on the geology map below.

Note 10. I suspect that most of the text was supplied by G. V. Maxted, who was keen to promote the virtues of the selected equipment. Of course, the crusher worked well only as long as all the hard material was hand-picked out! In other words it was under-powered / under-sized. If more substantial washmills were used (as was eventually the case), the crusher would in any case be unnecessary.

Note 11. This seems at first to be an odd statement. How thick is slurry? Surely it's as thick as you make it - depending on how much water you put in. The thicker the slurry is, the more power is needed to pump it. Underlying this is a fundamental problem in the psychology of the designers. See Note 16 below.

Note 12. The initial strategy in exploiting the Chalk Hill deposit was to drive a slot about 20 m wide along the northern property boundary, with a slight uphill trend.

Note 13. This must be the last slurry wheel installed - elevators were normally used if pumping was not possible.

Note 14. The separator (screener) was as supplied by Edgar Allen, but all suppliers provided separators along similar lines. Slurry particles needed to be below 0.125 mm for easy burning. The screens typically had 0.2 mm openings, this being the minimum size capable of withstanding the severely abrasive conditions, but the separator throws the slurry tangentially, and this reduces the effective size of the openings. Typical performance left about 5% above 0.09 mm.

Note 15. "Triple mixers" were obsolete. The later "sun and planet" and air-agitated mixers required an electric motor mounted on the turning boom. Before cheap electric motors became available, a design was required in which the agitation was supplied externally, originally from a steam-powered lay-shaft. Most of the slurry mixers installed in the 1920s - including Edgar Allen installations - were of the sun and planet type. The sun and planet mixer installed by Allen at Humber stirred 1000 m3 using a 25 HP motor. The Dunstable mixers used 20 HP motors to stir only half that amount.

Note 16. I wonder if they tried them with just one stirrer - or none at all! Maybe that would have been satisfactory too! Of course, removing a stirrer results in less-good mixing. Once again, the plant is either under-powered, or it is being mis-used.

Note 17. Here we find the root-cause of the problem. Perhaps by management fiat, they have decided that the slurry moisture content is to be 40%. After competent management took over the plant in the 1930s, Dunstable slurry moisture averaged 43.2%. The raw materials at Dunstable contain substantial amounts of swelling clay minerals resulting in relatively high viscosity for a given moisture content. The viscosity can always be reduced by raising the water content. For slurry such as that at Dunstable, the following relationship is typical:

slurry viscosity

The yield stress defines the power needed to pump the slurry. It can be seen that the yield stress is roughly halved for each 2% moisture increase. On the other hand, an additional 2% moisture raises the kiln energy consumption by 0.27 MJ/kg. In the present instance, excessively thick slurry is destroying the production equipment. Previous Allen installations had been at Sundon, Stockton, Barton, Barnstone and Humber. All except Sundon were capable of producing flowable slurry at moistures below 40%.

Note 18. The many sources of variation - the chemical variability of the two raw material sources, the variable moisture content of these, the variations in size of loads delivered, and the imprecision of the ratio control - no doubt had exactly the effect predictable. The normal strategy in such a system would be to accept the hour-to-hour variations, and to control the running mean of samples, making adjustments only if a "danger" level was reached. Such a strategy only works if there is plenty of capacitance in the blending system. In the absence of this, no amount of operator skill would be of avail. The triple mixers each held slurry equivalent to 300 tonnes of clinker (20 hours run) so there was plenty of capacitance available.

Note 19. Of the eight Edgar Allen installations of this period (Harbury, Dunstable, Barnstone, Sundon, Chinnor, Oxford, Gillingham and Rodmell), only Barnstone, Sundon and Gillingham had sun-and-planet basins for kiln feed storage - the others all had air-agitated silos of this sort. These each had a capacity of 525 m3 if filled to the recommended 5 ft from the top, and at the claimed moisture content contained 506 tonnes of dry material - enough to make perhaps 300 tonnes of clinker, or about 19 hours run of two kilns.

Note 20. Despite being described as "perfectly satisfactory", in view of the slurry viscosity problems, this is obviously an insanely bad technique. Since the only way of changing the kiln feed-rate was to physically change the orifice, this must have seriously discouraged the operator from making changes!

Note 21. In the 1930s, slurry sprays were replaced with chain systems, and conventional slurry spoon feeds were provided. The Rigby system is discussed in detail in the article on Harbury.

Note 22. Edgar Allen and Maxted were always dismissive of enlarged burning zones, but the majority of their installations had them - the only "parallel" kilns being Barnstone kiln 1, two at Humber, two at Dunstable and two at Oxford. None of the other suppliers provided parallel kilns during this period, so this opinion was not widely held. Parallel designs were, of course, much easier for the supplier. The odd diameter of the kilns - 9'8½" internal, 9'10" external - was never used before or subsequently.

Note 23. The kilns made around 190 t/day in the early years. The somewhat evasive statement of output, and the very slow kiln speed, suggests that the kilns were still struggling. The residence time was about 165 minutes.

Note 24. As with other Allen kilns of the time, the long belt in question extended from the electric motor at ground level to the gearbox on the third pier.

Note 25. Edgar Allen had exclusive rights for use of the Clarke Chapman Turbo-Pulverizer on cement plants. The combined fan/impactor was primarily designed for use in boiler firing, in which excess air was not a major concern, but in kiln firing, the amount of conveying air led to excessive primary air flowrate. Most installations were subsequently replaced with Atritors.

Note 26. So despite the fact that wet coal was no problem at all, they decided to put in a dryer! The plant started up in September 1926, during the May-October coal strike. Coal stocks had been built from March that year, and stockpiled coal was very wet by September. By the time the strike ended, standing stocks at collieries were also wet, so the problem continued into 1927.

Note 27. i.e. under the firing floor, as at Humber, Oxford, Gillingham and many early kiln installations. The coolers were not "parallel" - they had a 13 ft section of 8 ft diameter at the hot end, between two 5 ft long tapers. In addition to the 60 ft overall length, there was a 1.5 ft outlet grid.

Note 28. Although the term "volume" is used, these were weighers. They were used only intermittently, and were normally wheeled away from the cooler on rails, leaving the clinker to fall directly into the tray conveyor.

Note 29. Swing tray (shaker) conveyors were usually used only for clinker, because of their robust construction which could cope with occasional flushes of red hot material.

Note 30. Maxted and Knott were still using the box bin design used at Humber. These needed constant trimming to keep material moving. Furthermore, the capacity was very small. The bin held 750 tonnes of clinker, of which only 500 tonnes was "live" - or 32 hours kiln run. The design gave no blending effect at all, and most of the time, variable run-of-kiln clinker would have been ground.

Note 31. The live capacity was about 4500 tons. By 1926, all new installations used silos, usually of concrete. Edgar Allen, being a steel firm, preferred to supply steel silos.

Note 32. Of course this was never quantified, but from knowledge of the performance of modern electrostatic precipitators, when de-energised, it would be about 50%. This is why it was not a good idea to quantify it. The dust nuisance was considerable when the wind was in the wrong direction, although with the prevailing southwest wind, the down-wind area was sparsely populated at the time.

Note 33. Because of the low alkalis of Dunstable materials, this was a feasible expedient, although it probably resulted in yet more variability of the feed slurry viscosity. See Note 20.

Note 34. The Luton Municipal Electricity Undertaking commenced operation on 12/07/1901, using the Edison (DC) system. It was opened by Lord Kelvin. Part of its output was later converted to AC for industrial purposes. The system was extended to Dunstable (8 km from the power station) in 1925, and the cement plant project probably under-wrote this move.

Note 35. Equivalent modern EN 196 compression testing strength. The compressive strength data were obtained on the standard mix, which for the 1:3 sand mix was "earth-damp" with w/c ratio 0.3-0.4. This could lead to a much higher strength, but offset by poor compaction, it ends up about the same as the EN 196 value.

Note 36. This was later "Vitocrete" during the Red Triangle era, and "Ferrocrete" for Blue Circle. Dunstable's clinker was particularly bad for rapid hardening cement manufacture due to its low alkalis and sulfates. Like other RHPCs, its early strength was only high in comparison with the plant's OPC, which was uniquely low in 1-day strength.

Dunstable Geology

Dunstable geology LD

Geology of the area showing the locations of the three quarries employed. View in higher definition.

It can be seen from the section that the main quarry (A in the map) was not extended to the base of the Chalk Marl. This is explained by the chemistry of the material. The calcium carbonate contents of the strata are typically as follows:

Stratum% CaCO3
Upper Gray Chalk89
Middle Gray Chalk86
Lower Gray Chalk83
Totternhoe Stone78
Upper Chalk Marl74
Middle Chalk Marl67
Lower Chalk Marl60

The Gray Chalk in quarry A was mostly in the lower third of the Gray Chalk. The final rawmix was originally probably around 77.5% CaCO3 (rising to 78% later), so a roughly equal quantity of the upper marl only was needed to meet this composition.

At the outset (as described in the article) the marl was not accessible in quarry A, and so a small quarry B was developed at the foot of the ridge, allowing access to middle and lower marl. The use of this got through the Gray Chalk even more quickly (they say a 2 : 1 ratio). A spring at this location (developed into a well) resulted from a local down-warp of the strata, gathering the water that runs over the tops of the hard bands in the chalk. Quarry B was abandoned as soon as quarry A had been extended sufficiently down into the marl. By 1964, virtually all the available Gray Chalk was gone, and the plant started obtaining chalk from quarry C - the quarry of the old Sewell limeworks. This quarry was one of several in the area owned by Forder's, and so belonged to Blue Circle although it had remained dormant since the 1930s. This quarry has a complete section of the Gray Chalk, including the Plenus Marls at the top, and has the top of the Totternhoe Stone as floor. Chalk was washed to a slurry there and pumped to the main quarry washmills through a 1.2 km pipeline crossing the A5 on a bridge (500289,223536). By the time of closure in 1971, there was little high-grade remaining in either quarry.

During the life of the main quarry, the Totternhoe Stone was usually not used for cement. In this area it is particularly hard, and, as mentioned in the article, wet process equipment designed for handling very soft chalk was incapable of grinding it. At Sundon and Barrington, Totternhoe Stone was included in the mix. At Sundon at least, because the chalk contains no flint, some Totternhoe stone was considered essential in order to aid autogenous grinding in the washmill. At Dunstable, the hard rock was originally sidecast, but from 1936 to 1964 (when the stone in quarry A was worked out) it was used to make hydraulic lime. There were originally eight shaft kilns for this, later increased to fifteen, making about 18 t/day each. The kilns were supplied from the quarry by a ropeway over Houghton Road.