TWM537102U - Economical cycling system for preparing calcium sulfate crystal whiskers - Google Patents

Description

Calcium sulfate whisker economic cycle preparation system

This creation is about a whisker preparation system, especially a calcium sulfate whisker economic cycle preparation system.

Generally speaking, since the petrochemical industry usually burns petroleum coke to generate electricity, burning petroleum coke often produces a large amount of by-product lime (fly ash and bottom ash), which is a non-toxic commercial waste, but The annual production of by-product lime is several tens of thousands of tons. Therefore, even if part of the by-product lime is used for road backfilling, etc., it will not be able to effectively consume a large amount of by-product lime, resulting in a higher amount of by-product lime accumulation. The more you come, the more environmental hazards.

As mentioned above, although in the prior art, the prior art has used the by-product lime to produce calcium sulfate, and further to make calcium sulfate into gypsum board or floor tile, etc., due to limited demand for gypsum board or floor tile, it is still impossible. Effectively consumes by-product lime.

In view of the existing technology, the means for treating by-product lime is limited, and it is impossible to efficiently convert by-product lime into useful articles, thereby causing environmental hazards; thus, the main target of the creator of the present creation It is to provide a product which can effectively change the calcium sulfate further and has high economic value.

Based on the above objectives, the necessary technical means adopted by the present invention provides a calcium sulphate whisker economic cycle preparation system, which comprises a calcium sulphate slurry storage tank, a steam reaction kettle, a booster supply tank, and an acid addition pipeline. A catalyst supply tank.

The calcium sulphate slurry storage tank is used to provide a calcium sulphate slurry. The steam reactor is connected to a calcium sulfate slurry storage tank for receiving the calcium sulfate slurry. The auxiliary agent supply tank is connected to the steam reaction tank to provide a plurality of boosting agents to the steam reaction tank. The promoting agent comprises at least a sodium sulfate solution and a calcium oxide solution, and the sodium sulfate solution and the calcium oxide solution are connected to the steam reaction kettle. The reaction in the middle forms a plurality of calcium sulfate crystal nuclei. The catalyst supply tank is connected to the steam reactor to provide a catalyst to the steam reactor, and the steam reactor comprises a mixture of a calcium sulfate slurry, a calcium sulfate crystal nucleus and a catalyst. The acid addition pipeline is connected to the steam reactor for adding an acidic fluid to the steam reactor, so as to pass the calcium sulfate slurry in the mixture when the pH value of the mixture is adjusted between pH 2 and 4. The catalytic reaction with the catalyst causes the calcium sulphate nucleus to grow into a plurality of calcium sulphate whiskers.

The calcium sulfate crystal nucleus is passed through a catalytic reaction of the calcium sulfate slurry with the catalyst to form a plurality of calcium sulfate whiskers.

In an auxiliary technical means derived from the above-mentioned necessary technical means, the calcium sulfate whisker economic cycle preparation system further comprises a dehydration device connected to the steam reaction vessel for receiving one of the calcium sulfate whiskers. The whisker solution is dehydrated to separate the calcium sulfate whiskers. Preferably, the calcium sulfate whisker economic cycle preparation system further comprises a drying device for receiving calcium sulfate whiskers and drying the calcium sulfate whiskers. In addition, the calcium sulfate whisker economic cycle preparation system further comprises a recovery water tank connected to the dewatering device for recovering the water removed by the dewatering device.

In an auxiliary technical means derived from the above-mentioned necessary technical means, the auxiliary agent supply tank further provides a magnesium chloride solution, an ammonium chloride solution, a copper sulfate solution or a manganese sulfate solution.

In an auxiliary technical means derived from the above-mentioned essential technical means, the catalyst comprises a sodium chlorite solution or a potassium permanganate solution.

In an auxiliary technical means derived from the above-mentioned essential technical means, the calcium sulfate slurry comprises a calcium sulfate dihydrate slurry, a half water calcium sulfate slurry and an anhydrous calcium sulfate slurry.

In an auxiliary technical means derived from the above-mentioned necessary technical means, the calcium sulphate slurry storage tank is further connected to receive one calcium sulphate powder provided by the calcium sulphate preparation system, and the calcium sulphate slurry storage tank further comprises calcium sulphate powder. Water was added to prepare a calcium sulfate slurry for storage.

As described above, the calcium sulphate whisker economic cycle preparation system of the present invention mainly introduces calcium sulphate slurry, a growth promoter and a catalyst into a steam reaction kettle, and then synthesizes calcium sulfate whiskers with high economic value by hydrothermal method.

The specific embodiments used in the present application will be further illustrated by the following examples and drawings.

100‧‧‧ calcium sulfate preparation system

1‧‧‧Calcium-containing compound feed unit

11‧‧‧ powder storage tank

12‧‧‧Feed line

2‧‧‧Reaction tank

3‧‧‧ Crystallization tank

4‧‧‧ Acid supply unit

41‧‧‧ Acid storage tank

42‧‧‧First acid addition machine

43‧‧‧Second acid adding machine

5‧‧‧Cooling line

6‧‧‧Control module

61‧‧‧Monitoring pipeline

611‧‧‧pH meter

612‧‧‧ thermometer

62‧‧‧Control unit

7‧‧‧Exhaust gas treatment device

200‧‧‧calcium sulfate whisker economic cycle preparation system

201‧‧‧calcium sulphate slurry storage tank

202‧‧‧Steam reactor

203‧‧‧Promoter supply tank

204‧‧‧ Catalyst supply tank

205‧‧‧Adding acid pipeline

206‧‧‧Dewatering equipment

207‧‧‧Drying equipment

208‧‧‧Control unit

209‧‧‧Recycling sink

CC‧‧‧Calcium-containing compounds

CW‧‧‧calcium sulfate

CS‧‧‧ Calcium Sulfate Whiskers

CL1‧‧‧ Crystalline Precursor Solution

AC1‧‧‧ first acid solution

AC2‧‧‧Second acid

WS‧‧‧Water supply system

WG‧‧‧Exhaust

The first figure shows a system schematic diagram of a calcium sulphate preparation system provided by the preferred embodiment of the present invention; the second figure shows a system diagram of a calcium sulphate whisker economic cycle preparation system provided by the preferred embodiment of the present invention; The figure shows the temperature change diagram of the creation using the thermometer to detect the temperature change of the crystallization tank; and the fourth figure shows the pH change diagram of the creation using the thermometer to detect the pH change of the crystallization tank and control it.

Please refer to the first figure, which is a schematic diagram showing the system of the calcium sulfate preparation system provided by the preferred embodiment of the present invention. As shown, a calcium sulphate preparation system 100 includes a calcium-containing compound supply unit 1, a reaction tank 2, a crystallization tank 3, an acid supply unit 4, a cooling line 5, a control module 6, and a Exhaust gas treatment device 7.

The calcium-containing compound supply unit 1 comprises a powder storage tank 11 and a supply line 12, the powder storage tank 11 stores a calcium-containing compound CC, and the supply line 12 is connected to the powder storage material. The tank 11 is used to transport the calcium-containing compound CC. In practice, the calcium-containing compound CC contains a calcium-containing compound such as calcium carbonate, calcium hydroxide, calcium oxide, anhydrous calcium sulfate, and calcium sulfate, and the supply line 12 is transported by means of a transfer tube and a pump.

The reaction tank 2 is connected to the calcium-containing compound supply unit 1 The feed line 12 is configured to receive the calcium-containing compound CC and react the calcium-containing compound CC to form a crystalline precursor solution CL1 containing a plurality of calcium sulfate crystal nuclei. In practical use, the agitator is provided in the reaction tank 2, and the agitator is stirred at a rotational speed of 150 rpm to 300 rpm. Further, the reaction tank 2 is further connected to a water supply system WS in this embodiment, whereby water is added to the calcium-containing compound CC to form a crystal precursor solution CL1.

The crystallization tank 3 is connected to the reaction tank 2 for receiving the crystal precursor solution CL1, and the calcium sulfate crystal nucleus is combined with the calcium sulfate crystal crystallized by the crystal precursor solution CL1 to grow into a plurality of crystal grains of calcium sulfate CW. In practical use, the agitator is also provided in the crystallization tank 3, and the agitator is stirred at a speed of 150 rpm to 300 rpm.

The acid supply unit 4 includes an acid storage tank 41, a first acid addition machine 42, and a second acid addition unit 43. The acid storage tank 41 is for storing acid. The first acid adding machine 42 is connected to the acid storage tank 41 and the reaction tank 2, and supplies a first acid liquid AC1 to the reaction tank 2 from the acid liquid stored in the acid storage tank 41. The second acid adding machine 43 is connected to the acid storage tank 41 and the crystallization tank 3, and supplies a second acid liquid AC2 to the crystallization tank 3 from the acid liquid stored in the acid storage tank 41.

Wherein, the calcium-containing compound CC reacts with the first acid solution AC1 in the reaction tank 2 to form a crystal precursor solution CL1, and the second acid solution AC2 is used to control the pH value in the crystallizing tank 3 to make the crystal precursor The pH value of the solution CL1 in the crystallization tank 3 is maintained at a pH value suitable for the crystal growth of the calcium sulfate crystal nucleus, whereby the calcium sulphate crystal nucleus is calcium sulfate CW. In the present embodiment, the calcium sulfate CW is, for example, dihydrate. The crystal of calcium sulfate is not limited thereto.

In addition, in practice, the acid liquid stored in the acid storage tank 41 and the first acid liquid AC1 and the second acid liquid AC2 are both 50 wt% aqueous sulfuric acid solution, and the first acid liquid AC1 and the second acid liquid AC2 The difference is mainly that the first acid adding machine 42 adds the first acid liquid AC1 to the reaction tank 2 in an amount of 80% of the amount of the calcium-containing compound CC entering the reaction tank 2, that is, the first acid adding machine 42 is a calcium-containing compound CC. The amount of acid required for the reaction is fed to the reaction tank in a short time at a ratio of 80% to react with the calcium-containing compound CC; and the second acid solution AC2 is 20% of the amount of acid required for the reaction of the calcium-containing compound CC. The ratio is slowly introduced into the crystallization tank 3, and the pH value of the crystallization precursor solution CL1 in the crystallization tank 3 is controlled to be between pH 2 and 3; wherein, since the calcium-containing compound CC is in the reaction tank 2 Quickly react with an 80% reaction amount of acid in a short period of time (eg, within 10 to 60 minutes), thus producing a large amount of calcium sulphate nucleus, and when the calcium sulphate nucleus is in the crystallization tank 3, due to the second The acid adding machine 43 slowly adds the second acid liquid AC2 to the crystallization tank 3 at 20% of the reaction amount of the calcium-containing compound CC, so that the crystallization tank 3 is The pH value of the crystalline precursor solution CL1 is maintained between pH 2 and 3 suitable for the growth of the crystal, and the remaining 20% of the unreacted calcium-containing compound CC can be continuously reacted.

The cooling line 5 is for cooling the reaction tank 2 and the crystallization tank 3. Wherein, since the calcium-containing compound CC reacts with the first acid solution AC1 or the second acid solution AC2, the temperature in the reaction tank 2 and the crystallization tank 3 is increased due to the exothermic reaction, so that the reaction tank 2 and the crystallization tank are avoided. The reaction temperature in 3 is too high, and the temperature of the reaction tank 2 and the crystallization tank 3 is mainly controlled by the cooling water supplied from the cooling line 5, and the cooling water of the cooling line 5 is actually tap water or recycled water. But it is not limited to this.

The control module 6 includes a monitoring line 61 and a control unit 62. The monitoring line 61 is cyclically connected to the crystallization tank 3 for circulating the crystallization precursor solution CL1 in the monitoring line 61 and the crystallization tank 3, and the monitoring line 61 is provided with a pH meter 611 and a thermometer 612. The pH meter 611 is used to detect the crystal precursor solution CL1 flowing through the monitoring line 61 to obtain a crystal bath pH value. The thermometer 612 is used to detect the crystal precursor solution CL1 flowing through the monitoring line 61 to obtain a crystallization bath temperature value.

The control unit 62 is electrically connected to the pH meter 611, the thermometer 612, the second acid adding machine 43, and the cooling line 5. The control unit 62 receives the pH value of the crystallization tank detected by the pH meter 611, and controls the second acid adding machine 43 according to the pH value of the crystallization tank to adjust the rate at which the second acid solution AC2 enters the crystallization tank 3, thereby The pH value of the crystallization tank is controlled to be between pH=2 and 3. In addition, the control unit 62 controls the amount of cooling water flowing to the crystallization tank 3 by the cooling line 5 according to the crystallization tank temperature value, thereby controlling the temperature in the crystallization tank 3. Between 30 and 35 ° C.

The exhaust gas treatment device 7 is connected to the crystallization tank 3 for receiving the exhaust gas WG discharged when the crystal precursor solution CL1 reacts with the second acid solution AC2 to form the calcium sulfate CW in the crystallization tank 3, and treats the exhaust gas WG as non-toxic. The gas is then discharged into the air. In practice, when the second acid solution AC2 is added to the crystallization tank 3, the second acid solution AC2 is an aqueous solution of sulfuric acid, so that the exhaust gas WG of hydrogen sulfide (H ₂ S) gas is easily generated. Therefore, the hydrogen sulfide gas needs to be disposed of through the exhaust gas treatment device 7 to avoid environmental hazards. In practical application, the exhaust gas treatment device 7 utilizes an advanced oxidation technique to mainly generate a hydroxyl radical by reacting a pollution control neutralizer (HTS) with an oxidant (such as hydrogen peroxide, H ₂ O ₂ ) to utilize a hydroxyl group. The free radical oxidatively decomposes (substitutes or breaks) the organic matter in the exhaust gas WG into CO ₂ and H ₂ O, and is particularly effective for organic pollutants having high stability and being difficult to degrade.

Please refer to the second figure. The second figure shows that the present invention is a system schematic diagram showing the calcium sulfate whisker economic cycle preparation system provided by the preferred embodiment of the present invention. As shown, a calcium sulfate whisker economic cycle preparation system 200 includes a calcium sulfate slurry storage tank 201, a steam reactor 202, a booster supply tank 203, a catalyst supply tank 204, and an acid addition line 205. .

The calcium sulfate slurry storage tank 201 is used for providing a calcium sulfate slurry containing a calcium sulfate slurry, a half water calcium sulfate slurry and an anhydrous calcium sulfate slurry; in the present embodiment, calcium sulfate The slurry storage tank 201 is configured to receive the calcium sulfate CW prepared by the calcium sulfate preparation system 100, and the calcium sulfate slurry storage tank 201 is further connected to the water supply system WS, thereby modulating the calcium sulfate CW with water to prepare the calcium sulfate slurry. Save it. However, in other embodiments, the calcium sulphate slurry may also be prepared by adding 80% to 99% by weight of anhydrous calcium sulphate, calcium sulphate hemihydrate or calcium sulphate to water.

The steam reactor 202 is connected to the calcium sulfate slurry storage tank 201 for receiving the calcium sulfate slurry. In practice, the steam reactor 202 controls the crystal growth conditions in an environment of 90 ° C to 130 ° C and 0.1 MPa to 0.3 MPa.

The booster supply tank 203 is in communication with the steam reactor 202 for providing a plurality of boosters to the steam reactor 202 and providing a sodium sulphate solution and a calcium hydroxide solution promoting agent to react the sodium sulphate solution with the calcium oxide solution in the steam reactor 202 to form a plurality of calcium sulphate dihydrates; in addition, the growth agent supply tank 203 provides the growth The agent further comprises a magnesium chloride solution, an ammonium chloride solution, a copper sulfate solution or a manganese sulfate solution, wherein the magnesium chloride solution, the ammonium chloride solution, the copper sulfate solution and the manganese sulfate solution can dissolve magnesium ions and ammonia in the water. Root ions and sulfate ions, etc., therefore, the solubility of calcium sulfate slurry in water is improved by the same ion effect, and magnesium ions and copper ions are attached to the periphery of the calcium sulfate crystal nucleus, thereby increasing the crystal nucleus in a specific The surface energy in the direction causes the crystal to grow in one direction.

The catalyst supply tank 204 is connected to the steam reactor 202 for providing a catalyst to the steam reactor 202, and the steam reactor 202 comprises a mixture of a calcium sulfate slurry, a calcium sulfate crystal nucleus and a catalyst; The catalyst comprises a sodium chlorite solution or a potassium permanganate solution, but is not limited thereto. In practice, since the catalyst supply tank 204 provides the catalyst to the steam reactor 202, the steam reactor 202 maintains the growth conditions in the environment of 90 ° C to 130 ° C and 0.1 MPa to 0.3 MPa for 7 to 9 hours. At the time, the catalytic reaction through the catalyst causes the sulfate ion and the calcium ion provided by the calcium sulfate slurry to crystallize on the calcium sulfate crystal nucleus, and the growth promoter provided by the growth agent supply tank 204 can provide the crystal growth agent. In addition to the nucleus, the crystal growth direction of the crystal nucleus can be suppressed, and the calcium sulfate crystal nucleus is unidirectionally grown to form calcium sulfate whisker CS having a diameter of about 1 to 2 μm and a length of about 100 mm. In addition, in the present embodiment, the chemical reaction formula in the steam reactor 202 is mainly: (1) CaSO ₄ . 2H ₂ O dissolution process: CaSO4.2H ₂ O→Ca ²⁺ +SO ₄ ^2- +2H ₂ O; (2) CaSO ₄ . Crystallization of 0.5H ₂ O: Ca ²⁺ +SO4 ^2- +0.5H2O→CaSO ₄ . 0.5H ₂ O; (3) CaSO ₄ . Dehydration of 0.5H ₂ O to form anhydrous calcium sulfate whiskers: CaSO ₄ . 0.5H ₂ O→CaSO ₄ +0.5H ₂ O; thereby, the calcium sulfate whisker CS of the embodiment may be a calcium sulfate monohydrate or a anhydrous sulfuric acid, in addition to the calcium sulfate monohydrate. Calcium whiskers, and calcium sulfate dihydrate whiskers can be converted to calcium sulphate hemihydrate or calcium sulphate whiskers depending on the drying temperature.

The acid addition line 205 is in communication with the steam reactor 202 for adding an acidic fluid to the steam reactor 202, thereby permeable the sulfuric acid in the mixture while adjusting the pH of the mixture between pH 2 and 4. The catalytic reaction of the calcium slurry with the catalyst causes the calcium sulphate nucleus to grow into a plurality of calcium sulphate whiskers CS. In practical practice, the acid addition line 205 is particularly preferred to adjust the pH of the mixture between pH 3 and 4.

The dewatering apparatus 206 is connected to the steam reactor 202 for receiving a whisker solution containing calcium sulfate whiskers, and dehydrating the whisker solution to separate the calcium sulfate whiskers.

The drying device 207 is for receiving calcium sulfate whiskers CS and drying the calcium sulfate whiskers CS to produce calcium sulfate whiskers CS.

The control unit 208 is electrically connected to the steam reactor 202 for controlling the pH value and temperature of the mixture in the steam reactor 202. In addition, the steam reactor 202 is further provided with a stirrer, and the control unit 208 is more controllable. The agitator was stirred at a speed of from 100 rpm to 300 rpm. In practice, control unit 208 controls the amount of acidic fluid provided by acid addition line 205 into the tank of vapor reactor 202.

The recovery water tank 209 is connected to the dewatering device 206 and the calcium sulfate slurry storage tank 201 for recovering the water removed by the dewatering device 206, and supplies the recovered water to the calcium sulfate slurry storage tank 201 for the calcium sulfate slurry. The material storage tank 201 modulates calcium sulfate CW into a calcium sulfate slurry using recycled water. Further, in practical use, the recovery water tank 209 is further connected to the reaction tank 2 of the calcium sulfate preparation system 100 and the crystallization tank 3, whereby the reaction tank 2 prepares the calcium-containing compound CC into the crystal precursor solution CL1, and the crystallization tank 3 The concentration of the mixed solution in the crystallization tank 3 is adjusted.

As described above, the calcium sulphate whisker economic cycle preparation system 200 of the present invention mainly adds a calcium sulphate slurry, a growth promoter and a catalyst to the steam reactor 202, and further utilizes a hydrothermal method at 90 ° C to 130 ° C and 0.1 MPa. Calcium sulfate whiskers CS with high economic value were synthesized in a 0.3 MPa environment for 7 to 8 hours.

Please continue to refer to the third and fourth figures. The third figure shows the temperature change diagram of the creation of the temperature change of the crystallizing tank by the thermometer and the temperature change. The fourth figure shows that the creation uses the thermometer to detect the pH of the crystallizing tank. A change in pH value that changes and controls the value. As shown in the figure, in actual operation, the calcium sulphate preparation system 100 of the present invention is further provided with another thermometer and another pH meter in the reaction tank 2 to detect the formation of crystals of the calcium-containing compound CC in the first acid solution AC1. After the precursor solution CL1, the process of adding the second acid solution AC2 is continued; as shown in the third figure, the crystal precursor solution CL1 is added from the calcium-containing compound CC to the first acid solution AC1 to form the crystal precursor solution CL1 within 1 hour. The temperature rises above 43 ° C, then cools to below 35 ° C through the cooling line 5, and then continues to add the second acid liquid AC2, then the temperature Control is between 32 ° C and 35 ° C.

As described in the fourth figure, the pH of the crystal precursor solution CL1 is reduced to about 2 hours after the calcium-containing compound CC is added to the first acid solution AC1 to form the crystal precursor solution CL1, and then continuously added. In the case of the second acid solution AC2, the pH is controlled between 2 and 3.

As described above, the yield of the calcium-containing compound CC converted to calcium sulfate CW can be as high as 90% or more by the above temperature and pH control. Further, as is apparent from the third and fourth figures, the temperature and the pH value in the crystallization tank 3 have been stabilized in about 3 hours, that is, the reaction has been completed.

In summary, the calcium sulphate whisker economic cycle preparation system of the present invention mainly adds a calcium sulphate slurry, a growth promoter and a catalyst into a steam reaction kettle, and then synthesizes calcium sulfate whiskers by hydrothermal method, and calcium sulfate crystals. The requirement has high economic value because it can effectively improve the strength, stability, toughness and flame resistance of the plastic; thus, this creation can effectively convert calcium sulfate into high economic value compared with the prior art. The calcium sulfate whisker effectively solves the problem of environmental damage caused by limited consumption of by-product lime.

The features and spirit of the present invention are more clearly described in the above detailed description of the preferred embodiments, and the scope of the present invention is not limited by the preferred embodiments disclosed herein. On the contrary, it is intended to cover all kinds of changes and equivalences within the scope of the patent application to which the present invention is intended.

200‧‧‧calcium sulfate whisker economic cycle preparation system

201‧‧‧calcium sulphate slurry storage tank

202‧‧‧Steam reactor

203‧‧‧Promoter supply tank

204‧‧‧ Catalyst supply tank

205‧‧‧Adding acid pipeline

206‧‧‧Dewatering equipment

207‧‧‧Drying equipment

208‧‧‧Control unit

209‧‧‧Recycling sink

CS‧‧‧ Calcium Sulfate Whiskers

CW‧‧‧calcium sulfate

WS‧‧‧Water supply system

Claims (9)

A calcium sulfate whisker economic cycle preparation system, comprising: a calcium sulfate slurry storage tank for providing a calcium sulfate slurry; a steam reaction tank connected to the calcium sulfate slurry storage tank for receiving the a calcium sulphate slurry; a booster supply tank connected to the steam reactor for providing a plurality of boosting agents to the steam reactor, the boosting agent comprising at least a sodium sulphate solution and a calcium sulphate solution, The sodium sulphate solution and the calcium oxide solution are reacted in the steam reactor to form a plurality of calcium sulphate crystal nucleus; and a catalyst supply tank is connected to the steam reactor to provide a catalyst to the steam reactor. The steam reactor comprises a mixture of the calcium sulphate slurry, the calcium sulphate nucleus and the catalyst; an acid addition line is connected to the steam reactor for adding an acidic fluid to the The steam reactor, whereby the sulfuric acid base of the mixture is adjusted between pH 2 and 4, and the sulfuric acid slurry in the mixture is catalyzed by the catalyst to react the sulfuric acid with the catalyst. The calcium nucleus grows into a plurality of calcium sulfate whiskers. The calcium sulphate whisker economic cycle preparation system according to claim 1, further comprising a dehydration device connected to the steam reaction vessel for receiving a whisker solution containing the calcium sulphate whiskers, and The whisker solution is dehydrated to separate the calcium sulfate whiskers. The calcium sulphate whisker economic cycle preparation system according to claim 2, further comprising a drying device connected to the dehydration device for receiving the calcium sulphate whiskers and the calcium sulphate whiskers Dry. The calcium sulfate whisker economic cycle preparation system according to claim 2, further comprising a recovery water tank connected to the dewatering device for recovering moisture removed by the dewatering device. The calcium sulfate whisker economic cycle preparation system according to claim 1, wherein the growth agent supply tank further provides at least one of a magnesium chloride solution, an ammonium chloride solution, a copper sulfate solution and a manganese sulfate solution. By. The calcium sulphate whisker economic cycle preparation system according to claim 1, wherein the catalyst comprises at least one of a sodium chlorite solution and a potassium permanganate solution. The calcium sulfate whisker economic cycle preparation system according to claim 1, wherein the calcium sulfate slurry comprises a calcium sulfate dihydrate slurry, a half water calcium sulfate slurry, and an anhydrous calcium sulfate slurry. The calcium sulfate whisker according to claim 1 of the patent application scope The calcium sulphate preparation system, wherein the calcium sulphate slurry storage tank is further connected to receive one calcium sulphate powder provided by the calcium sulphate preparation system, and the calcium sulphate slurry storage tank further modulates the calcium sulphate powder into water The calcium sulfate slurry is stored for storage. The calcium sulphate whisker economic cycle preparation system according to claim 1, further comprising a control unit electrically connected to the steam reaction vessel for controlling the pH value of the mixture in the steam reactor With temperature.