Production of stabilized wet process phosphoric acid

Abstract

This invention is directed to improvements in making wet process phosphoric acid substantially free from post-precipitation. The improvements include recycling to the reaction train a side stream produced by the process; cooling one or more of the streams of the process; and/or addition of sulfuric acid to an evaporator.

Description

This invention is directed to improvements in the process of preparing a merchant grade wet process phosphoric acid with good post-precipitation control. In one aspect the improvement involves recycling back into the reaction train a side stream which is produced in the process.

Another improvement contemplated in the process is cooling certain of the streams in the process to cause additional precipitation of solids, thereby permitting removal of additional solids in the operation of the process.

Still another improvement is the addition of sulfuric acid to an evaporator (apparatus used in the process) to improve post-precipitation control when high iron and alumina rock is used as feed.

The basic process (herein, the "Basic Process") of which this invention is an improvement or improvements is described in my U.S. Pat. No. 4,110,422, and also in my copending U.S. applications Ser. Nos. 951,804, filed Oct. 16, 1978 and 883,381, filed Mar. 6, 1978. A related application is Ser. No. 54,449, filed July 3, 1979, for "Stabilized Wet Process Phosphoric Acid", Docket 5588. The entire disclosures of said patent and said applications are incorporated herein by reference.

The Basic Process includes several essential steps. A dilute phosphoric acid analyzing 22-46% P.sub.2 O.sub.5 is thoroughly clarified to the extent feasible. Then aluminum silicate is added thereto in an amount of about 1 to 40 pounds of aluminum silicate per ton of equivalent P.sub.2 O.sub.5 in the acid. The aluminum silicate is preferably perlite. The acid is then concentrated, typically up to about 45-52% P.sub.2 O.sub.5, and is then sent to a crystallizing zone, where it is allowed to deposit crystals. The overflow stream, containing at most a small amount of crystals, can be taken as final product, or it can be further concentrated, e.g., up to 52-54% P.sub.2 O.sub.5 for merchant grade acid or (preferably) up to 57-63% P.sub.2 O.sub.5 to constitute the final product. The underflow stream from the crystallizer can be about 0.5-15 wt. % of the incoming feed to the crystallizer; preferably the range is 1-8%, and even more preferably it is 2-6%. Present commercial plant experience indicates 6% to be typical. This underflow stream contains in solution about the same percentage of P.sub.2 O.sub.5 as in the feed to the crystallizer and about the same percentage of P.sub.2 O.sub.5 as in the outgoing overflow stream. In addition it contains solids, and these solids may contain 10-45% P.sub.2 O.sub.5, and 20-25% P.sub.2 O.sub.5 is typical.

In view of the content of P.sub.2 O.sub.5 in the underflow stream from the crystallizer, this stream should not be wasted. This invention, inter alia, is directed to a process for recovering this stream by returning it back to the acid train.

By acid train is meant the entire series of steps for making wet process phosphoric acid that precede the formation of the crystals in the crystallizer, starting with the so-called "head box". Basically these steps include a mix tank wherein dilute sulfuric acid and phosphate rock are mixed. This reaction product proceeds to a digester where the reaction continues, and the digester effluent is filtered to provide a filter cake of gypsum and a filtrate of dilute crude phosphoric acid. This dilute acid proceeds to a clarifier, the underflow of which is returned to the train, and the overflow is concentrated in stages to 40%, then to 50%, and then goes to the crystallizer, and then is concentrated possibly to 60%. (These percentages are approximate.) There are generally a number of intermediate operations. For example, there may be several mix tanks, one feeding into the other, as well as two or more digesters, with effluent from one going into the other. The head box above mentioned collects reaction product slurry taken from one of the digesters and may also include underflow from the clarifier and washings from the filtering operation. It is a preferred embodiment of this invention that the crystallizer underflow be returned to the launder mixer feeding to the clarifier. However, it may be returned to other unit operations of the train, including the head box, a mix tank, a digester, or the feed line going to the filter.

In another embodiment the final filtrate product from the filter operation is cooled before it is clarified. This decreases the solubility of the saturated components, thereby precipitating them, and causing them to be caught in the clarifier. In another, similar, operation after the aluminum silicate-containing acid is concentrated, it is cooled before it is sent to the crystallizer settler. Each of these two cooling operations can be used alone, or in combination with each other, or in combination with the return of the underflow from the crystallizer back to the acid train. Preferably all three embodiments are used together. Also, they can be used singly or in any permutation with the improvement involving sulfuric acid addition above referenced. When high iron and aluminum rock is used as feed, all four embodiments are preferably used together. Each cooling operation can be carried out at 40-60.degree. C., preferably 50-55.degree. C.

Reference is made to the drawing which is a diagrammatical flow sheet of a large scale plant utilizing the process of the instant invention. Much of the overall process is conventional. At 1 is shown the head box. This is the initial vessel for receipt of several streams. One such stream is stream 3, from flash cooler 7, which receives recycled slurry via line 5 from the second digester 49. A vacuum line 9 maintains a reduced pressure on the flash cooler. Line 11 feeding into the head box 1 is from clarifier 89, further described below. Line 13 is return acid from the No. 2 filtrate, also described below. Proceeding now with the basic operation of the wet process phosphoric acid plant, phosphate rock is fed via line 17 into rock feeder 19, from which rock exit line 21 delivers metered amounts of phosphate rock into first mix tank 25. Exit line 23 delivers liquid from the head box 1 also into mix tank 25. Sulfuric acid via line 27 and water via line 29 are fed into dilution cooler 31, and this diluted sulfuric acid proceeds via line 33 to two branches, lines 35 and 37, each of which feeds respectively into a mix tank, line 35 feeding into mix tank 25 and line 37 into mix tank 41. The effluent from mix tank 25 exits via line 39 into mix tank 41, and the effluent from mix tank 41 exits via line 43 into first digester 45, from which exit line 47 feeds into second digester 49. Some of the slurry from digester 49 is returned via line 5 to head box 1 as already mentioned. The rest of the effluent from the second digester flow via line 51 into filter feed tank 53, from which the exits at line 55 into the prayon filter, shown here schematically in sections identified simply as 57, 59, and 61. Each section actually undergoes the steps of taking a first filtrate, followed by washing, followed by passing the wash water through a second operation, and the return of the resulting weak acid to the head box. These steps are further described as follows: Effluent line 55 from the filter feed tank proceeds to prayon filter 57, where it is filtered, and the No. 1 filtrate is delivered via line 63 into collection tank 65, from whence the effluent proceeds via line 67, to operations to be subsequently described. Wash water is fed via line 79 through the gypsum filter cake sitting on the filter leaf, as shown at 61, and the effluent waters pass via line 73 as No. 3 filtrate to collection vessel 75. The effluent line from vessel 75, line 77, containing the No. 3 filtrate, passes through another gypsum filter cake, at 59, and the washings are taken via line 69 to form No. 2 filtrate. The No. 2 filtrate is collected in vessel 71, and returned via line 13 to the said box 1 as already described. The filtration sequence is thus filtration through filter 57, which then becomes filter 59 and is washed with the No. 3 filtrate, following which filter No. 59 becomes filter 61, which is washed with plain wash water (typically pond water) to provide No. 3 filtrate used in the preceding step, which preceding step provides No. 2 filtrate which is returned to the head box. Returning now to line 67, No. 1 filtrate, this will proceed to launder mixer 85, where it is mixed with flocculation polymer, prepared as an aqueous solution in tank 81 and pumped via line 83 to the launder mixer. Line 84 carries underflow from crystallizer-settler 109 to launder mixer 85. The effluent line 87 from the launder mixer feeds to clarifier 89, which has overflow 91 and underflow 11. Overflow 91 feeds to a surge tank 97. Effluent from the surge tank 97 is pumped via line 99 to perlite addition tank 100. Perlite or other aluminum silicate is fed via line 95 to perlite feeder 96, which exits via line 94 to line 99. Sulfuric acid may also be added to mix tank 100 via line 98. Tank 100 (which is agitated) exits to a first evaporator (herein "E") 101. Here the acid is concentrated up to about 40% P.sub.2 O.sub.5. Effluent proceeds via line 103 to a second evaporator (herein "F") 105, where it is concentrated up to about 48-52% P.sub.2 O.sub.5. Line 104 may feed sulfuric acid into evaporator 105. Effluent line 107 takes the acid from evaporator 105 via line 107 to crystallizer-settler 109, which has overflow line 111 and underflow line 84. Overflow line 111 feeds to surge tank 113, and the effluent from the surge tank is taken by line 115 to branches 117 and 119. If the product is not to be concentrated further, commercial product can be taken out of line 117. If the product is to be concentrated further it is taken via line 119 to a third evaporator (herein "G") 121. Effluent line from evaporator 121, namely line 123, is the final product line. Concentration in evaporator 121 typically proceeds to a P.sub.2 O.sub.5 content within the range of 52 to 63. Sulfuric acid line 129 may feed into line 107, for use with high iron and alumina rock, as elsewhere herein explained. Sulfuric acid may also be fed into the final product via line 131.

Crystallizer Underflow Return

The return of the crystallizer underflow to the acid train is one of the preferred embodiments of this invention.

My analyses from pilot plant work suggest that the solid product of the crystallizer is an undefined conglomerate, mostly of iron, calcium, and aluminum phosphates; calcium sulfate, and fluoride; and with minor amounts of insoluble complex phosphates and/or fluorides of sodium, potassium, strontium, titanium, and magnesium. This composition is suggested by the following typical analyses of solids taken from the pilot plant crystallizer underflow. As is evident, analyses for the same sample can vary considerably, depending on preparation, washing, etc.

One sample of crystallizer solids, immediately below, was centrifugally filtered. It was done this way in order to obtain a cake with a low content of liquid. The cake was removed and assayed "as is". This is sample No. 1. Part of this cake was also acetone washed and assayed without removing the excess acetone. This is sample No. 2. Data are in weight percent.

______________________________________ No. 1 No. 2 (As Is) (Acetone Washed)______________________________________P.sub.2 O.sub.5 46.50 41.00CaO 3.51 3.90SiO.sub.2 0.13 0.21Fe.sub.2 O.sub.3 8.22 15.10Al.sub.2 O.sub.3 1.02 3.35F 1.23 2.04H.sub.2 SO.sub.4 9.03 12.83MgO 0.40 0.22Na.sub.2 O 0.63 1.03K.sub.2 O 0.73 0.78______________________________________ Another sample was also centrifugally filtered, but this time washed with water while still being centrifuged. The cake was again divided, one sent to analysis "as is", the other acetone washed. These are Nos. 3 and 4 respectively. ______________________________________ No. 3 No. 4 (As Is) (Acetone Washed)______________________________________P.sub.2 O.sub.5 30.20 38.35CaO 3.96 11.05SiO.sub.2 0.02 0.03Fe.sub.2 O.sub.3 9.62 15.25Al.sub.2 O.sub.3 0.67 3.25F 0.27 0.41H.sub.2 SO.sub.4 13.51 17.16MgO 0.03 0.02Na.sub.2 O 0.29 0.33K.sub.2 O 0.77 0.79______________________________________

Another underflow sample was obtained which was an accumulation of the settled crystals over the 2nd and 3rd shifts on one day and the first part of the 1st shift on the following day. I sent to analysis a sample "as is" (No. 5) from the "head sample" above described.

______________________________________ No. 5 Underflow As Is______________________________________P.sub.2 O.sub.5 44.40CaO 2.61SiO.sub.2 1.90Fe.sub.2 O.sub.3 3.39Al.sub.2 O.sub.3 1.50F 3.39H.sub.2 SO.sub.4 7.94MgO 0.59Na.sub.2 O 0.74K.sub.2 O 0.38Solids 23.87______________________________________

Four additional samples of about 400 cc each were centrifugally filtered. The first sample was centrifuged only, producing a cake and a filtrate. These are Nos. 6 and 7. The second was washed with 600 cc water only. The cake is No. 8 while the filtrate, which is now a mixture of the displaced acid and water, is No. 9. The next sample was washed with 400 cc acetone and the last with alcohol. These are identified at the head of each column (Nos. 10-13).

______________________________________ No. 8 No. 9No. 6 No. 7 Water Washed AcidCake Filtrate Cake +As Is (Acid Only) (Not Dried) Water______________________________________P.sub.2 O.sub.5 33.75 47.50 24.75 28.80CaO 8.46 0.17 10.04 0.23SiO.sub.2 0.95 0.12 5.17 0.29FE.sub.2 O.sub.3 6.75 1.16 8.30 0.61Al.sub.2 O.sub.3 2.10 1.47 1.80 0.85F 8.15 0.68 9.01 0.68H.sub.2 SO.sub.4 1.39 4.30 1.52 2.90MgO 0.58 0.59 0.51 0.40Na.sub.2 O 0.77 0.07 0.76 0.34K.sub.2 O 0.50 0.03 0.52 0.03______________________________________ ______________________________________No. 10 No. 12Cake No. 11 Cake No. 13(Acetone Filtrate (Alcohol FiltrateWashed- (Acid Washed- (AcidVacuum + Vacuum +Dried) Acetone) Dried) Alcohol)______________________________________P.sub.2 O.sub.5 29.88 34.60 27.38 37.80CaO 11.77 0.08 12.81 0.06SiO.sub.2 6.02 0.12 6.93 0.00Fe.sub.2 O.sub.3 10.05 0.76 10.75 0.80Al.sub.2 O.sub.3 0.43 0.96 1.65 1.08F 9.47 0.46 10.78 0.49H.sub.2 SO.sub.4 19.31 3.00 20.56 3.30MgO 0.65 0.45 1.61 0.48Na.sub.2 O 0.13 0.06 0.78 0.04K.sub.2 O 0.14 0.02 0.53 0.02______________________________________

As above noted, in a preferred embodiment the crystallizer underflow (line 84) is returned to the launder-mixer 85, where it is mixed with flocculant and the No. 1 filtrate, for feeding to the clarifier 89. There are, however, other effective places upstream in the train where the underflow can be added, namely, to the head box 1, where it is mixed with recycled reaction slurry and filtrate washings; and/or to the filter feed tank 53. Also, the stream can be divided, for return to two or more of those positions.

When the underflow from the crystallizer-settler 109 is returned to the clarifier 89, e.g., via launder mixer 85, or to the stilling well of the clarifier, I prefer to add flocculant polymer, suitably Polyhall M295, at the rate of 0.1% by weight in water, then add the solution to the mixing launder 85 with the acid (line 67) at 1% by volume of the acid. The polymer should be completely in solution before it is used. I also prefer to add a 50% NaOH solution into the launder, at the rate of about 3.2 pounds of 100% NaOH per ton of P.sub.2 O.sub.5 in the acid. These embodiments greatly improve the quality of the clarifier overflow 91.

In an alternate preferred embodiment, which works as well as or better than returning the crystallizer-settler underflow to the clarifier launder-mixer 85, the underflow from the crystallizer-settler is pumped to the stilling well in the clarifier. The strong underflow acid is displaced from the crystallizer-settler underflow solids with 28% acid and these solids, comingled with the solids from the solids from the clarifier, are pumped as clarifier underflow to the digestion circuit (line 11).

Since the liquid portion of the crystallizer underflow return is about 50% P.sub.2 O.sub.5 acid, this serves to raise the P.sub.2 O.sub.5 in the clarifier, e.g., in the overflow, to about 30%.

By this method I have eliminated "in plant" sludge. Also by this method I do not lose evaporative capacity which occurs when the crystallizer-settler underflow is returned to digestion directly.

It is best to have the concentration of crystallizer-settler solids as high as possible and still be fluid enough to pump. The underflow from the crystallizer-settler has been as high as 35% solids by wt., but a better operating range is 20 to 25% by wt. The underflow from the clarifier has been as high as 45%, but about 30 to 35% by wt. is more easily handled. It does no harm to pump lower solids content; this merely increases the acid recycle.

In commercial scale performance, the initial routing of crystallizer underflow (line 84) to clarifier 89 via launder 85 resulted in an increase in solids in clarifier overflow (from 0.1% to 0.5% solids). It was anticipated that this change might also result in higher solids in the "F" evaporator product (line 107), the crystallizer overflow (line 111) and the "G" evaporator product (line 123). However, each of these three latter lines actually showed a decrease in solids. The reasons were not clear; possibly the decrease was not related to passing the crystallizer underflow to the clarifier, since at the same time addition of a descaler (to descale the evaporator tubes) was discontinued. With continued elimination of the descaler, solids in the 3 indicated lines began to increase and eventually attained expected but acceptable levels (typically 1.0-1.4%). Thus, overall, no deterioration in performance was detected by reason of returning crystallizer underflow to the clarifier, and the benefit of the change, i.e., making the circuit integral by consuming a by-product line, was readily achieved. The final product resulting from the return is apparently indistinguishable from the product resulting from the process without the crystallizer underflow return.

The crystallizer-settler 109 used in the commercial application of my invention had an overall diameter of 35 feet by 20 feet high, with a total volume of about 144,000 gallons. With an acid feed rate of 46 GPM the total displacement time is about 2.13 days. At 61 GPM this becomes 1.64 days. The bottom of the crystallizer within the settler is 16'-4" below the surface of the acid. This is the point at which the incoming acid leaves the crystallizer and starts its upward journey through the settler to the outlets. This volume, which I refer to as the active volume, is approximately 117,000 gallons or a retention time at 47 GPM of 1.73 days compared to 1.33 days at 61 GPM. The additional aging at the lower rate may be helpful, particularly if the operator skips from one rock blend to another at odd times. Three to 4 days aging may be beneficial. Some rock blends produce acid that do much better in the crystallizer-settler if cooled first. Bench scale tests show that if the acid is cooled to about 35 to 40.degree. C. the small amount of light brown solids that settle after 4 to 5 days in the final product can be dramatically reduced.

Lab tests have also shown that P.sub.2 O.sub.5 concentration to the crystallizer-settler can influence the quality of underflow. Lower P.sub.2 O.sub.5 to the crystallizer-settler, i.e., 47 to 48% produces less iron whereas if the P.sub.2 O.sub.5 is increased to 50% the iron in the underflow increases.

As already indicated, aluminum silicate (preferably perlite) acts as an aid to crystal growth and formation, causing more rapid settling in the crystallizer-settler 109.

Cooling the Acid

Cooling the acid as herein described is another preferred embodiment of the invention.

It is of advantage to cool (e.g., to down to 35-60.degree. C., or preferably, 50-55.degree. C.) the dilute phosphoric acid feed to the clarifier and/or feed to the crystallizer settler. In each instance additional solids are precipitated for recovery and removal from the system. These additional solids are believed to be mostly calcium sulfate and sodium potassium, and calcium silicofluoride. This embodiment can be used with or without the return of the crystallizer underflow upstream to the train. However, preferably this embodiment is used with crystallizer underflow return.

Sulfuric Acid Addition to the Crystallizer

This is a preferred embodiment of the invention and is particularly useful when the reaction train uses phosphate rock high in iron and aluminum ("high I and A"). Such rock may analyze typically

______________________________________ Wt. %______________________________________ P.sub.2 O.sub.5 32.4 CaO 46.2 SiO.sub.2 5.3 Fe.sub.2 O.sub.3 1.59 Al.sub.2 O.sub.3 1.44 F 3.47 H.sub.2 SO.sub.4 1.6 MgO 0.32 Na.sub.2 O 0.49 K.sub.2 O 0.06 SO.sub.3 1.28______________________________________

Rock in which the ratio of Fe.sub.2 O.sub.3 plus Al.sub.2 O.sub.3 to P.sub.2 O.sub.5 exceeds 0.08 is considered "high I and A" rock. Thus, in the above rock, (Fe.sub.2 O.sub.3)+Al.sub.2 O.sub.3)/P.sub.2 O.sub.5 =(1.59+1.44)/32.4=0.094, which puts it in the category of "high I and A" rock.

The Basic Process as described in my U.S. Pat. No. 4,110,422 as applied to high I and A rock can be considerably improved if the sulfate content in the crystallizer effluent is maintained at 6-15% of the P.sub.2 O.sub.5 content of the acid exiting the crystallizer. If sulfate measured as H.sub.2 SO.sub.4) is below this level, it can be brought up by adding sulfuric acid to the crystallizer, e.g., by line 129. Such sulfuric acid is suitably 93% concentration. The amount to be added is determined by the sulfate content and volume of the incoming stream (line 107), the sulfate analysis desired in the crystallizer overflow, and the acid concentration in line 129. In this embodiment, 6-10% is preferred, and about 8% is more preferred.

Some experimentation may be desirable as regards a given phosphate rock to determine the minimum amount of perlite or other aluminum silicate that can be used. The rock used in the process described in my U.S. Pat. No. 4,110,422 was known as "Bonny Lake" rock, a local Florida rock. Phosphoric acid made from Bonny Lake rock ordinarily requires only about 4-6 pounds of perlite/ton P.sub.2 O.sub.5, and H.sub.2 SO.sub.4 adjustment is not necessary. The "high I and A" rock above reported is from the so-called "Hookers Prairie" area (another Florida rock) and phosphoric acid from Hookers Prairie rock typically requires 12-16 lb. perlite/ton P.sub.2 O.sub.5 in the acid, plus preferably H.sub.2 SO.sub.4 adjustment upward to about 8% as aforesaid, based on P.sub.2 O.sub.5 in the acid. While the reason the addition of sulfuric acid helps control post-precipitation is not entirely clear, there is evidence to the effect that it may help prevent crystallization of iron hydrogen phosphate and its analog aluminum hydrogen phosphate. The higher perlite requirement for acid from Hookers Prairie rock may also be associated with an arbitrarily shorter residence time in the crystallizer-settler 109. By way of comparison, Bonny Lake rock was run at 38-40 tons of rock one hour through the train described in the drawing, versus 44 tons/hour for Hookers Prairie rock. Accordingly it would appear that the higher perlite requirement for Hookers Prairie rock may be related to lessened residence in the crystallizer-settler.

The products made by the herein described improvements are about the same as those made by the Basic Process, as described in my applications and patent above referenced, and for a detailed description of those products reference is made thereto.

By way of summary, the following may be mentioned.

The products of this invention, e.g., those in Table A, are characterized by the following features: (a) such solids as exist are suspended and nearly non-settling; (b) such solids as exist are soft, free flowing, and non-caking; (c) the solids-containing acid is readily pumped from storage and does not form a cake over outlets, valves, and accessory mechanisms; (d) the acid can be ammoniated without substantial foaming. The above criteria apply to acids of this invention in lab samples and/or shipped and stored in conventional equipment and for normal use times, e.g., in tank cars, typically of 200,000 lbs.

In the specification and claims all percentages are by weight unless otherwise stated.

TABLE A______________________________________Some Products of This Invention "High P.sub.2 O.sub.5 " "Low P.sub.2 O.sub.5 " Low-high Acid Acid range,Component Wt. % Wt. % Wt. %______________________________________P.sub.2 O.sub.5 58-61 52-55 52-63Solids 0-2 0.5-3 0-3SO.sub.4 as H.sub.2 SO.sub.4 3.5-5 2.5-5.5 2.5-6.0CaO 0.05-1 0.09-0.4 0-1.2SiO.sub.2 0.02-0.15 0.03-0.25 0-0.25F 0.5-1.5 0.9-1.3 .35-1.5Fe.sub.2 O.sub.3 1.1-2 1-3 .5-3Al.sub.2 O.sub.3 1.1-2 1-3 .5-3Na.sub.2 O 0.025-0.15 .04-0.09 .02-0.2K.sub.2 O 0.025-0.15 0.01-0.12 0.01-0.2MgO 0.5-0.65 0.35-0.6 0.3-0.7Sum of CaO, SiO.sub.2,F, Na.sub.2 O, K.sub.2 O, andMgO 1.1-3.6 1.4-2.8 0.7-4______________________________________

The problem of post precipitation in prior art 52-54% P.sub.2 O.sub.5 merchant grade acid is bad enough; it is impossible with prior art 60% acid, as the post precipitation in such 60% acid is even worse, and for that reason (prior to my invention of the Basic Process) 60% merchant grade acid was not ordinarily available commercially for shipment over any considerable distance or storage for any substantial time.

The tank car cleaning problem with prior art sludge is particularly aggravated in that harsh measures (scraping, chipping) tend to penetrate the rubber lining of the car. This cleaning "fact of life" necessitates great caution and prolonged cleaning times.

Aside from the augmented post-precipitation problems of an ordinary 60% P.sub.2 O.sub.5 merchant grade acid, such product is technically very difficult to make using prior art 50% P.sub.2 O.sub.5 feed acid. The latter tends to boil and entrain in the 60% evaporator. This behavior is quite aside from its post precipitation problems. On the other hand, my 50% product from line 111 from crystallizer 109 is readily concentrated in the "G" evaporator 121, to 57-63% without boiling or entraining.

In a series of runs during the initial operation of a 70,000 ton/year wet process phosphoric acid plant using the Basic Process, extending over a period of a little over two months, 47 daily samples were taken from "G" evaporator product (line 123), and analyzed for P.sub.2 O.sub.5 and solids (inter alia). The average (mean) of the 47 runs was 59.72% P.sub.2 O.sub.5. A particularly suitable P.sub.2 O.sub.5 range was 59-61%. The values above 61% were 5 runs at 61.5% and one run at 62%. There were 10 runs below 59% namely two at 56, one at 56.5, two at 57, one at 57.5, three at 58, and one at 58.5. The average (mean) of the 47 runs was 1.3% solids. The three lowest values were 0.5, 0.5, and 0.6%. The three highest values were 2.1, 2.2, and 5%. Sampling and/or analytical errors may have been involved in the 5% report. A range of about 0.8-1.8% solids was typical for a P.sub.2 O.sub.5 range of 59-61%. During the later months of operation, after the plant achieved optimum performance under preferred conditions, as hereinafter described, solids for 58-60 % P.sub.2 O.sub.5 acid dropped to an average of about 0.14 wt. %, with a range of 0-1.1 wt %.

The P.sub.2 O.sub.5 in the final product can be controlled with a fair degree of precision, simply by evaporating more or less water from the product in the final concentration stage. The exact amount of solids and of other components is a consequence of all the preceding steps in the process, and cannot be predetermined with certainty. These values will, however, normally and inherently fall within the ranges here stated, if the process is operated as herein described. For example, the operator cannot "aim" specifically at a product with exactly 0.14% solids. However, proper operation of the process as described will in general result in a product carrying solids of about 0-2%, so that his desired solids percentage will not be far from his actual result.

The reason why the suspended solids do not readily settle out (as they do in ordinary 52-54% P.sub.2 O.sub.5 merchant grade acid) is not entirely clear. One reason is apparently that the solid particles in my product are unusually small, being an estimated 5 microns. Also, they are of relatively low density (about 2). These factors contribute to their enduring suspension, especially in 57-63% acid (density about 1.8).

The advantages of the phosphoric acid products of the Basic Process and of this invention may be demonstrated with respect to their behavior on shipment in standard phosphoric acid tank cars. These tank cars slope gently from the ends toward the center, to a sump, to which is attached a discharge pipe, closed by a dismountable flange, and equipped with a valve. The tank car is equipped with a dip tube which is closed by a flange; the car has a rupture diaphragm, a man hole access, and various convenience equipment including ladder, and hand rail. The flange can be removed for unloading.

Phosphoric acid is corrosive, and will corrode the tank car unless the latter is protected by a coating. Conventionally this coating is a rubber lining, 1/4 inch thick. The coating covers the interior of the tank car. When a tank car of ordinary wet process merchant grade phosphoric acid is shipped, it begins to lay down a deposit of sludge. Owing to the motion of the car, the layer tends to deposit not only on the bottom of the car but also will coat the front and rear ends, as well as the sides. This layer can become quite thick, e.g., up to 36 inches in aggravated cases.

In shipping ordinary merchant grade acid, sludge tends to collect in the sump and the exit pipe, and to foul the valve. This is in addition to settling on the bottom and sides of the tank car as already described. This fouling gives an immediate problem on attempting to empty the car via the discharge pipe. Since the caked sludge around the exit equipment first has to be broken up. This work typically requires one to two hours. Even after the initial clearances have been made, additional pieces of sludge and cake might flow into the valve and exit pipe, slowing or blocking flow of the acid.

There are two ways to remove acid from a tank car. One way is through the sump out the bottom, as already described. The other way is through the dip tube. In order to manage this the cover flange is removed, a conduit is attached, and compressed air is blown in. Again, this procedure requires that the dip tube terminus at the bottom of the tank car be free of cake. If it is not free, it has to be made free. This may be accomplished by the use of an air lance. If that doesn't work, the dip tube may have to be pulled out. These procedures are time-consuming and frustrating.

Neither of the two aforesaid procedures for draining prior art acid from a tank car are effective for removing the layer of sludge deposited on the bottom and sides by ordinary merchant acid. This layer is a hard cake in most cases, and cannot be flushed out easily. Men have to enter the tank car physically with cleaning equipment to dislodge this cake. Aside from the time, effort and inconvenience involved in cleaning out the cake, following removal of the acid from the tank car, there is a severe economic loss represented by the amount of cake that is left. Prior art merchant grade acid typically deposited 5 to 10% of its P.sub.2 O.sub.5 content as sludge, which caked up in the car and was unavailable to deliver to the customer, since the customer pays only for the acid pumped from the car. The cake that is left is for the account of and is the responsibility of the seller. Since phosphoric acid may sell at $250.00 per ton of P.sub.2 O.sub.5, it is evident that the loss per tank car might run $500.00 to $1000.00. This loss is doubly unfortunate, since the sludge has value by reason of its P.sub.2 O.sub.5 content.

The instant products (especially the 58-63% P.sub.2 O.sub.5 products) differ from the prior art products inter alia in their freedom from depositing cake and sludge that prevent recovery of solids. By way of contrast with prior art wet process acids, the acids of this invention can be pumped instantly from tank cars, even after the cars have been in transit or in storage for several weeks. My products do not clog valves or exit lines, and do not substantially settle out in transit and/or storage. The small amount of sediment that does deposit is not of a caking type, and is readily washed out. Practically all solids in my products that are in the products when made and shipped out from the commercial phosphoric acid plant stay suspended in the acid during transit and/or storage and become thus available to the customer. This is, of course, advantageous to the customer, who has the advantage of the P.sub.2 O.sub.5 content of the small amount of suspended solids in my products, and it is likewise economically advantageous to the manufacturer, who does not have to absorb the loss of sludge unrecoverable and unsaleable at the point of destination.

A certain small amount of solids can be tolerated in merchant grade phosphoric acid prepared in accordance with my invention without causing any problem in post precipitation. For example, acid made by my process may on occasion show a solid content as high as 3% in the finished acid as shipped, analyzing 52 to 63% P.sub.2 O.sub.5. However, my pre-treatment operations to prevent post precipitation have the result that most of these solids stay in suspension in the acid. For example, as the acid sits in a tank car for weeks on end, only minimal amounts of solids precipitate. Even these minimal amounts do not drop out as sludge, but rather as a thin covering on the rubber lining of the tank car, readily removed when the car is pumped out.

Unloading a tank car of normal merchant grade phosphoric acid usually requires a considerable period of time just getting the acid to flow. Sludge deposits over unloading valve act like a plug and must be broken through. Operators will hook air to the valve and blow out the plug if possible. An air lance, down the dip pipe, is used sometimes to clear the valve. With evaporator product it has been necessary to drive a bar up through the valve to get flow started. It is not unusual to spend two hours getting the flow started. If the car has not been cleaned on the last couple of trips, sludge can stop flow and the procedure must be redone. Time required to start flow ranges from thirty minutes to two hours. After flow is started, pumping requires two hours minimum. Washing of cars requires about thirty minutes to set up and four to sixteen hours to wash sludge from cars. Some cars will have four feet of solids in the ends and this is very difficult to remove. The sludge is hard and comes loose in chunks that must be broken up by the acid jet. It is a difficult and time consuming job.

In contrast, acid prepared in accordance with the Basic Process and by this invention (especially 58-63% P.sub.2 O.sub.5) flows as soon as bottom car valve is open. No lance, air blow or rodding is required. Pumping time has averaged one hour and twenty minutes per car. Cars carrying such acid have required only a simple rinse to remove the inch (approximate) of solids in cars. The preparation time for wash is still required but the actual wash is very small.

Analytical

Except for solids and iron, analyses were made by procedures in "Methods Used and Adopted by the Association of Florida Phosphate Chemists", Fifth Ed., 1970 ("AFPC"). Where more than one method is provided, the selections were as follows:

P, Photometric method (phosphate rock), p. 80.

Aluminum oxide, Atomic absorption method, p. 95.

F, Specific ion electrode method, p. 104A.

Water, Karl Fischer method, p. 127.

Phosphoric acid in phosphoric acid, Total phosphoric acid method, p. 132.

Solids were determined by the following procedure:

Apparatus

a. Vacuum filtration system

b. Drying oven adjusted to 105.degree. C.

c. Gooch crucible, porcelain, with perforated bottom

Reagents

a. Asbestos--Powminco brand or equivalent, special for Gooch crucibles, acid washed. This grade asbestos as received should be thick slurried with water and blended in a Waring blender or equivalent for 10 seconds. The blended slurry should then be placed in an Erlenmeyer flask and washed 3-5 times by adding distilled water and decanting to remove the extremely fine material. The washing is accomplished by thoroughly shaking the blended asbestos with each water wash and then allowing it to settle for 5-10 minutes before decantation of the excess water and fine material.

b. Methanol, absolute

Determination

Prepare the Gooch crucible with a pad of asbestos which filters freely under medium suction. (In lieu of asbestos, glass fibers can be used.) Pad should be thick enough to retain all suspended solids. Wash pad several times with distilled water, finally with methanol, and place in drying oven at 105.degree. C. for a minimum of one hour. Remove from drying oven and place in desiccator until cool. Reject or rework crucibles which visually show evidence of pad separation from crucible walls. Weigh crucible rapidly and record tare weight. Resuspend solids in sample by shaking thoroughly. Immediately weigh approximately five-ten grams of sample, accurately weighed, into the crucible. Place the crucible and contents on a filter flask and filter with strong vacuum until all of the liquid portion has been filtered through. Wash the solids five times with five ml portions of methanol allowing each wash to filter through completely. Remove crucible from suction and place in the drying oven at 105.degree. C. for a minimum of one hour. Cool in desiccator and weigh rapidly as soon as cool. ##STR1##

In these analyses, samples are well shaken, then immediately analyzed. Thus, values for P.sub.2 O.sub.5, lime, silica, iron, alumina, etc. include components in both liquid and solid phases.

Ferrous and ferric iron were determined by the following procedure:

Reagents

a. Standard Potassium Dichromate

A 0.1 N solution is made by dissolving 4.904 grams and diluting to one liter with distilled water.

b. Stannous Chloride

Sixty grams of the crystallized salt is dissolved in 600 ml of concentrated HC1 and made up to 1 liter with distilled water.

c. Phosphoric Acid--Sulfuric Acid Mixture

150 ml concentrated H.sub.2 SO.sub.4 and 150 ml concentrated H.sub.3 PO.sub.4 are diluted to 1 liter with distilled water.

d. Mercuric Chloride

A saturated solution of HgCl.sub.2 (60-70 grams per liter) is made.

e. Diphenylamine

One gram of diphenylamine is dissolved in 100 ml of H.sub.2 SO.sub.4.

Determination

A 5.00 gram sample of acid is weighed into a 250 ml beaker. About 100 ml of distilled water is added to the beaker. Then 15 ml of the phosphoric-sulfuric acid mixture and 4 drops of diphenylamine are added. The solution is stirred and potassium dichromate is added drop by drop until a deep purple color develops. The milliliters of potassium dichromate is recorded and used in the calculation for ferrous iron. A total iron is run by weighing out 5.00 grams into a 250 ml beaker, adding 25 ml of 1:1 HCl and about one ml of 2% potassium permanganate solution, placing this on the hot plate and boiling until the color of permanganate is destroyed. The iron is then reduced by adding stannous chloride drop by drop until the solution is colorless. Add one-two drops in excess. The solution is allowed to cool to room temperature. The solution is diluted to 100 ml and 15 ml saturated mercuric chloride is added. Add 15 ml of phosphoric-sulfuric acid mixture and 4 drops of diphenylamine indicator. Potassium dichromate is added drop by drop to the stirred solution until a deep purple end point develops. ##EQU1##

Preferred embodiments for operating the commercial plant above described (cf. the drawing) include:

(1) using a 50/50 mix of Hookers Prairie (so-called) (HP) phosphate rock and Bonny Lake (BL) rock (from the Central Florida area). The analyses of these two rocks are typically:

______________________________________ HP BL______________________________________P.sub.2 O.sub.5, wt % 32.4 31.40CaO 46.2 47.3SiO.sub.2 5.3 8.56Fe.sub.2 O.sub.3 1.59 0.89Al.sub.2 O.sub.3 1.44 0.90F 3.47 3.57SO.sub.4 as H.sub.2 SO.sub.4 1.6 0.73MgO 0.32 0.33Na.sub.2 O 0.49 0.59K.sub.2 O 0.06 0.35______________________________________

(2) Perlite use, at the rate 16 lb./ton of P.sub.2 O.sub.5 in the crude acid at the perlite addition vessel.

(3)NaOH addition to clarifier, at the rate of 3 lbs. (Na.sub.2 O equivalent) per ton of P.sub.2 O.sub.5 in the crude acid in the clarifier. (NaOH is preferred to Na.sub.2 CO.sub.3 for addition to the clarifier.)

(4) Sulfuric acid addition to crude phosphoric acid stream to first evaporator, at the rate of 8% H.sub.2 SO.sub.4 based on the weight of P.sub.2 O.sub.5 of the phosphoric acid at this point.

(5) Fe in the rock feed comprises mostly ferric Fe with possibly some ferrous Fe. The ferrous/ferric ratio may appear in the acid (No. 1 filtrate) going to the clarifier as

Ferrous Fe, 1.69 g./liter Ferric Fe, 8.35 g./liter

Using the above preferred conditions, a series of 35 consecutive runs was carried out (per the drawing) to make 58% P.sub.2 O.sub.5 acid. The average (mean) solids in this series was 0.14%, with a range of 0% to 1.1%. Solids were measured on samples taken from a tank receiving effluent from line 193, FIG. 4. The tank had a capacity equivalent to five days normal production (at 70,000 tons/year), i.e., about 21 tank cars. However, owing to rapid turnover, it generally carried only about four tank cars.

Claims

1. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train, comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid in a clarification zone, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5, and passing the concentrated acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising returning the said crystals-containing stream to the acid train.

2. Method according to claim 1, in which the crystals-containing stream is admixed with the dilute acid prior to clarification.

3. Method according to claim 1 in which the crystals-containing stream is returned to the reaction zone.

4. Method according to claim 3 in which the crystals-containing stream is mixed with recycled reaction slurry and filtration washings before passing it to the reaction zone.

5. Method according to claim 1 in which the crystals-containing stream is returned to the filtration zone.

6. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train, comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5, and passing the concentrated acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising cooling the filtered acid to a temperature in the range of 35.degree.-60.degree. C. before clarifying it.

7. Process according to claim 6 in which the filtered acid is cooled to a temperature in the range of 50.degree.-55.degree. C.

8. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train, comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5 and passing the concentrated acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising cooling the concentrated acid to a temperature in the range of 40.degree.-60.degree. C. before passing it to the crystallizing zone.

9. Process according to claim 8 in which the improvement additionally comprises cooling the filtered acid to a temperature in the range of 35.degree.-60.degree. C. before clarifying it.

10. Process according to claim 8 or claim 9 in which the temperature is 50.degree.-55.degree. C.

11. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train, comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5, and passing the concentrated acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising (a) cooling the filtered acid to a temperature in the range of 35.degree.-60.degree. C. before clarifying it, and (b) returning the said crystals-containing stream to the acid train.

12. Process according to claim 11 in which the temperature range in (a) is 50.degree.-55.degree. C.

13. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train, comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5, and passing the concentrated acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising (a) cooling the concentrated acid to a temperature in the range of 35.degree.-60.degree. C. before passing it to the crystallizing zone, and (b) returning the said crystals-containing stream to the acid train.

14. Process according to claim 13 in which the temperature in (a) is 50.degree.-55.degree. C.

15. Process according to claim 13 in which the improvement additionally comprises cooling the filtered acid to a temperature in the range of 35.degree.-60.degree. C. before clarifying it.

16. Process according to claim 15 in which the filtered acid is cooled to 50.degree.-55.degree. C.

17. Process according to claim 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, or 16, in which the crystals-containing stream is mixed with the dilute acid prior to clarification.

18. In the process of preparing wet process phosphoric acid with low post-precipitation characteristics in an acid train comprising preparing dilute phosphoric acid by reaction of sulfuric acid and phosphate rock high in iron and alumina in a reaction zone to form a reaction slurry, filtering the reaction slurry in a filtration zone to provide a filtered acid, clarifying the filtered acid, adding aluminum silicate to the clarified acid, concentrating the acid to about 45-52% P.sub.2 O.sub.5, and passing the concentraed acid to a crystallizing zone to provide a product stream and a stream containing most of the crystals produced in the crystallizing zone, said crystals analyzing 10-45% P.sub.2 O.sub.5 and being mostly phosphates; the improvement comprising adding sulfuric acid to the concentrated acid being passed to the crystallizing zone to raise the sulfate content of that acid up to about 6-15% of the P.sub.2 O.sub.5.

19. Process according to claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, or 17 in which the phosphate rock is high iron and aluminum rock and sulfuric acid is added to the concentrated acid being passed to the crystallizing zone to raise the sulfate content thereof up to about 8% of the P.sub.2 O.sub.5.

20. Method according to claim 2 in which flocculant polymer is added to the clarifier as about a 0.1% by weight water solution, said solution being about 1% by volume of the phosphoric acid feed to the clarifier, together with an aqueous solution of sodium hydroxide at the rate of about 3.2 pounds NaOH, 100% basis, per ton of P.sub.2 O.sub.5 in the acid.

21. Method according to claim 1 in which the crystals-containing stream is returned to the clarification zone.