CN116059805A - A method for preparing acid gas drying dehydrating agent from waste dechlorination agent - Google Patents

Abstract

The present disclosure relates to a method for preparing an acid gas dry dehydrating agent from a spent dechlorinating agent, the method comprising: s1, performing first roasting treatment on a waste dechlorinating agent in an inert atmosphere to obtain a first material; s2, carrying out filtration washing after carrying out immersion treatment on the first material in acid liquor to obtain a second material; s3, drying and second roasting the second material; wherein the spent dechlorinating agent comprises oxides and hydroxides of calcium, aluminum oxide, sodium oxide, magnesium oxide, ferric oxide and calcium chloride. With the acid gas desiccant of the present disclosure, the hydrogen chloride content in the gas is unchanged while dehydration occurs, and the replenishment of chlorine can be reduced.

Description

A method for preparing acid gas drying dehydrating agent from waste dechlorination agent

technical field

The disclosure relates to the field of desiccant preparation, in particular to a method for preparing acid gas drying dehydrating agent from waste dechlorination agent.

Background technique

For modern refineries, continuous reforming has become an important technology for the production of aromatics and high-octane gasoline. It is also the main source of hydrogen for hydrogenation units. The smooth operation of catalytic reforming units directly affects the economic benefits of the entire refinery.

In recent years, reforming technology, especially continuous reforming, has developed rapidly, and the related supporting technology-dechlorination technology is an indispensable technology. There are 4 parts of the reforming unit that need to use dechlorination technology, namely: (1) pre-hydrogenated refined stone Naphtha dechlorination technology; (2) Dechlorination technology for reforming hydrogen production; (3) Removal technology for chlorine in reforming oil; (4) Continuous reforming regeneration unit for recycling regeneration gas and releasing chlorine in air removal technique.

The reforming raw material needs hydrofining treatment to meet the requirements of the reforming catalyst. The chlorine content in the pre-hydrogenation raw material is as high as 150 μg/g or even higher depending on the raw material. During the pre-hydrogenation reaction, the organic chloride is hydrogenated Generate hydrogen chloride, and react with ammonia generated in the pre-hydrogenation process to generate ammonium chloride. Ammonium chloride deposits in a low-temperature environment, causing corrosion and blockage of heat exchange, air coolers, and low-temperature parts of water coolers. In order to eliminate the above-mentioned chlorine A dechlorination reactor is added after the prehydrogenation reactor, and the solid dechlorination technology is used to remove the hydrogen chloride in the prehydrogenation product by using the residual heat of the prehydrogenation reaction, so as to protect the normal operation and operation of downstream devices and equipment. performance of the associated catalyst.

For the reforming unit, whether it is a semi-regenerated or continuous reforming catalyst, chlorine components will continue to be lost. In order to maintain the catalytic performance of the reforming catalyst, it is necessary to continuously inject organic chlorides during operation to control the balance of water and chlorine. The catalyst The lost chlorine components exist in reformed hydrogen and reformed oil in the form of hydrogen chloride. When this reformed hydrogen containing trace amounts of hydrogen chloride is supplied to downstream devices, it will bring (1) hydrogen chloride will cause corrosion of downstream equipment; (2) combine with trace amounts of nitrogen to form ammonium chloride, which will cause blockage of cooling equipment and circulating compressors , fouling, and there are major hidden dangers in the safe operation of the device. At the same time, a small amount of hydrogen chloride will be adsorbed by the catalyst in the downstream hydrogenation unit, which will affect the performance of the hydrogenation catalyst. Therefore, measures must be taken to remove hydrogen chloride in the reformed hydrogen to eliminate its influence. The solid dechlorination technology of reforming hydrogen can well solve the above problems.

The chlorine in the reformed oil is lost to the oil during the operation of the reforming catalyst, and the content will gradually increase with the increase of the operating time of the reforming catalyst, and the fluctuation range is 1 μg/g to 4 μg/g. The existence of the depentanizer and the debutanizer will cause corrosion of the cooling equipment at the top of the depentanizer. When the reformed oil contains high ammonium ions, it will combine with hydrogen chloride to form ammonium chloride, which will be on the top of the depentanizer and debutanizer. The low-temperature part of the top of the alkane tower is gradually deposited, and the accumulation to a certain extent will cause equipment blockage. It may also exist in the dry gas of the reforming unit, which will cause the blockage of the heating furnace nozzle and affect the normal operation of the reforming unit. In this case In recent years, it often occurs in CCR units (especially those with large processing capacity). In addition, when reformed oil is used as raw material for aromatics extraction, chlorine will affect the adsorption performance of aromatics adsorbent. In summary, , It is necessary to adopt solid dechlorination technology for the reformed oil to remove the chlorine in the oil.

Whether it is UOP CCR, Axens CCR or domestic CCR technology, catalyst regeneration technology is one of its core technologies. Disadvantages of alkali washing to remove chlorine include large equipment investment, complex process flow, difficult operation and control technology, waste water alkali slag needs to be treated, and equipment corrosion still exists. After 2000, the solid dechlorination technology of regenerated gas gradually replaced the alkali elution of chlorine, and achieved better results.

Although the solid dechlorination technology used in catalytic reforming units has unique technical advantages such as simple dechlorination process, convenient operation and monitoring of dechlorination units, and accurate product detection, due to the rapid development of reforming units, especially continuous reforming technology, in recent years, The annual consumption of dechlorination agent in the supporting dechlorination device is also increasing. In 2020, the consumption of dechlorination agent is expected to be about 15,000 tons. Since the dechlorination agent is a one-time use product, it cannot be reused through regeneration. It means that about 15,000 tons of waste dechlorination agents need to be disposed of every year. The current common method is to bury it as a hazardous waste. Not only does it cost a lot to bury it, but it also has a potential impact on the environment, which is not in line with the concept of green development in the petrochemical industry.

During the application of the dechlorination agent, due to system corrosion and other reasons, the processed raw materials contain impurities such as rust, and these reaction products will be deposited on the dechlorination agent, affecting the dechlorination performance of the dechlorination agent and the reuse of the waste dechlorination agent. .

The dechlorination principle of the dechlorination agent is to use the structure of the dechlorination agent and the active component (such as calcium) to make hydrogen chloride adsorb on the dechlorination agent or react with the active component to form chloride and fix it on the dechlorination agent, so in dechlorination In the reactor bed, the dechlorination agent that first contacts with hydrogen chloride reacts or absorbs hydrogen chloride first, and the dechlorination reaction is a piston reaction from top to bottom. Since the contact time between the dechlorination agent and hydrogen chloride in the lower part of the bed is reduced, its The dechlorination performance is limited by the overall dechlorination effect, and the active components such as calcium in the dechlorination agent still exist as part of metal oxides or hydroxides, which will also affect the drying and dehydration performance of the dechlorination agent.

Contents of the invention

The purpose of the disclosure is to reuse the waste dechlorination agent, which reduces the disposal cost of the waste dechlorination agent and the pollution to the environment.

In order to achieve the above object, the first aspect of the present disclosure provides a method for preparing an acid gas drying dehydrating agent from a waste dechlorination agent, the method comprising:

S1. Carrying out the first roasting treatment on the waste dechlorination agent under an inert atmosphere to obtain the first material;

S2. Dip the first material in an acid solution and then filter and wash it to obtain a second material;

S3, performing drying treatment and second roasting treatment on the second material;

Wherein, the waste dechlorination agent contains calcium oxide and hydroxide, aluminum oxide, sodium oxide, magnesium oxide, ferric oxide and calcium chloride.

Optionally, based on the total weight of the waste dechlorination agent, the weight percent of calcium oxide and hydroxide is 8-70wt%, the weight percent of aluminum oxide is 30-80wt%, and the weight percent of sodium oxide is 0.4-8wt%, the weight percent of magnesium oxide is 0.3-2wt%, the weight percent of ferric oxide is 0.5-2wt%, the weight percent of calcium chloride is 20-75wt%; preferably, the oxide of calcium and hydrogen The weight percent of oxide is 10-65wt%, the weight percent of aluminum oxide is 35-75wt%, the weight percent of sodium oxide is 0.5-5wt%, the weight percent of magnesium oxide is 0.5-1.5wt%, the weight percent of ferric oxide The weight percentage is 1-1.6 wt%, and the weight percentage of calcium chloride is 35-70 wt%.

Optionally, the inert atmosphere is selected from one of nitrogen atmosphere and argon atmosphere, preferably nitrogen atmosphere.

Optionally, the pH value of the acid solution is not greater than 3, and the acid solution is selected from hydrochloric acid.

Optionally, in step S1, the conditions of the first roasting treatment include: the temperature is 450-550°C, preferably 480-520°C; the time is 3-6 hours, preferably 4-5 hours; in step S2, The conditions of the dipping treatment include: the temperature is 30-80°C, preferably 50-60°C; the time is 2-5 hours, preferably 3-4 hours; in step S3, the conditions of the drying treatment include: the temperature is 100-130°C, preferably 110-120°C; the time is 2-5 hours, preferably 3-4 hours; the conditions of the second roasting treatment include: the temperature is 400-500°C, preferably 430-450°C; The time is 2-5 hours, preferably 3-4 hours.

The second aspect of the present disclosure provides an acid gas drying and dehydrating agent.

Optionally, the acid gas drying and dehydrating agent contains 35-70% by weight of calcium chloride.

Optionally, the acid gas drying and dehydrating agent has a particle size of 1-5 mm, preferably 2-4 mm; a specific surface area of 30-100 m ² /g, and a total pore volume of 0.15-0.35 cc/g.

The third aspect of the present disclosure provides a method for drying and dehydrating acid gas containing hydrogen chloride, which is characterized in that the acid gas is contacted with an acid gas drying and dehydrating agent for dehydration and drying.

Optionally, the dehydration and drying conditions include: a temperature of 50-200° C., preferably 150-180° C., and a pressure of 0.1-1.0 MPa, preferably 0.3-0.8 MPa.

Optionally, the method further includes: when the water content in the acid gas passing through the acid gas desiccant is greater than 50 μg/L, regenerating the acid gas drying and dehydrating agent;

Optionally, the regeneration conditions include: roasting the acid gas drying dehydrating agent to be produced in a nitrogen atmosphere; optionally, the roasting temperature is 260-310°C.

Through the above technical scheme, the disclosed method can prepare the waste dechlorination agent used by the reforming dechlorination device into an acid gas drying dehydrating agent after impurity purification treatment and component optimization, so that the waste dechlorination The chlorine agent is reused, eliminating or reducing the disposal cost of the waste dechlorination agent and the pollution to the environment. The dry dehydrating agent can remove water in acid gas containing hydrogen chloride, for example, it can remove water in acid gas containing 1-12% water and 1-3000μg/L hydrogen chloride to 10-50μg/L, and the dehydrated gas The hydrogen chloride content remains unchanged, and the dry dehydrating agent also has good regeneration performance and can be used repeatedly.

Other features and advantages of the present disclosure will be described in detail in the detailed description that follows.

Detailed ways

Specific embodiments of the present disclosure will be described in detail below. It should be understood that the specific embodiments described here are only used to illustrate and explain the present disclosure, and are not intended to limit the present disclosure.

In order to achieve the above object, the first aspect of the present disclosure provides a method for preparing an acid gas drying dehydrating agent from a waste dechlorination agent, the method comprising:

S1. Carrying out the first roasting treatment on the waste dechlorination agent under an inert atmosphere to obtain the first material;

S2. Dip the first material in an acid solution and then filter and wash it to obtain a second material;

S3, performing drying treatment and second roasting treatment on the second material;

Wherein, the waste dechlorination agent contains calcium oxide and hydroxide, aluminum oxide, sodium oxide, magnesium oxide, ferric oxide and calcium chloride.

The specific purification and component optimization method of the acid gas desiccant prepared by the waste dechlorination agent of the present disclosure is to treat the waste dechlorination agent at high temperature under a nitrogen atmosphere, remove the oil gas adsorbed by the waste dechlorination agent, and then The hydrochloric acid solution treatment removes the iron rust on the waste dechlorination agent, and at the same time, the calcium oxide and calcium hydroxide in the hydrochloric acid and the waste dechlorination agent that do not react with hydrogen chloride are further reacted and converted into calcium chloride, which is washed, filtered, and dried. Roasting at high temperature removes the bound water of calcium chloride, and the waste dechlorination agent becomes a product mainly composed of anhydrous calcium chloride, thereby obtaining the acid gas desiccant prepared from the waste dechlorination agent of the present disclosure.

The waste dechlorination agent described in this disclosure is the dechlorination agent discarded after the dechlorination agent of the solid dechlorination device of the reforming unit fails, including the high-temperature dechlorination agent of the pre-hydrogenation product, the reforming hydrogen dechlorination agent, and the reformed oil Liquid dechlorination agent and continuous reforming regeneration unit cycle regeneration gas and air dechlorination agent, especially suitable for high temperature dechlorination agent of prehydrogenation product, high temperature dechlorination agent of regenerated flue gas of reforming unit and reforming hydrogen dechlorination agent.

According to the present disclosure, based on the total weight of the waste dechlorination agent, the weight percent of calcium oxide and hydroxide can be 8-70wt%, the weight percent of aluminum oxide can be 30-80wt%, and the weight percent of sodium oxide can be 8-70wt%. 0.4-8wt%, the weight percent of magnesium oxide is 0.3-2wt%, the weight percent of ferric oxide is 0.5-2wt%, the weight percent of calcium chloride is 20-75wt%; preferably, the oxide of calcium and The weight percent of hydroxide is 10-65wt%, the weight percent of aluminum oxide is 35-75wt%, the weight percent of sodium oxide is 0.5-5wt%, the weight percent of magnesium oxide is 0.5-1.5wt%, the ferric oxide The weight percent of calcium chloride is 1-1.6wt%, and the weight percent of calcium chloride is 35-70wt%.

According to the present disclosure, the inert atmosphere may be selected from one of nitrogen atmosphere and argon atmosphere, preferably nitrogen atmosphere.

According to the present disclosure, the pH value of the acid solution is preferably not greater than 3, and the acid solution may be selected from hydrochloric acid.

According to the present disclosure, in step S1, the conditions of the first calcination treatment include: the temperature is 450-550°C, preferably 480-520°C; the time is 3-6 hours, preferably 4-5 hours; in step S2, The conditions of the dipping treatment include: the temperature is 30-80°C, preferably 50-60°C; the time is 2-5 hours, preferably 3-4 hours; in step S3, the conditions of the drying treatment include: the temperature is 100-130°C, preferably 110-120°C; the time is 2-5 hours, preferably 3-4 hours; the conditions of the second roasting treatment include: the temperature is 400-500°C, preferably 430-450°C; The time is 2-5 hours, preferably 3-4 hours.

The second aspect of the present disclosure provides an acid gas drying and dehydrating agent.

According to the present disclosure, the acid gas drying and dehydrating agent may contain 35-70% by weight of calcium chloride.

According to the present disclosure, the particle size of the acid gas drying and dehydrating agent may be 1-5 mm, preferably 2-4 mm; the specific surface area is 30-100 m ² /g, and the total pore volume is 0.15-0.35 cc/g.

The acid gas desiccant disclosed in the present disclosure can be used in the drying and dehydration working conditions of the regeneration unit of the continuous reforming device, and can also be used in the drying and dehydrating working conditions of other similar gases.

The third aspect of the present disclosure provides a method for drying and dehydrating an acid gas containing hydrogen chloride, which is characterized in that the acid gas is contacted with a dehydration drying agent for dehydration and drying.

According to the present disclosure, the dehydration and drying conditions may include: a temperature of 50-200° C., preferably 150-180° C., and a pressure of 0.1-1.0 MPa, preferably 0.3-0.8 MPa.

The acid gas desiccant prepared by the waste dechlorination agent of the present disclosure can be in contact with the acid gas at 50-200°C, preferably at 150-180°C, and remove the water in the regeneration gas from 1-12% to Below 50μg/L, while the hydrogen chloride in the regeneration gas remains unchanged, which greatly reduces the supplement of chlorine. On the basis of the reuse of the waste dechlorination agent, the consumption of chlorine is also reduced, and the environmental protection level of the device is improved.

The acid gas desiccant prepared by the waste dechlorination agent of the present disclosure also has excellent regeneration performance. As a preferred embodiment of the present disclosure, the method further includes: when the acid gas passing through the acid gas desiccant When the water content is greater than 50 μg/L, the acid gas drying and dehydrating agent is regenerated.

Preferably, the regeneration conditions may include: treating the acid gas desiccant for adsorbing water of the present disclosure with nitrogen gas at a temperature of 260-310°C, preferably 290-300°C, to remove the adsorbed water, Can be reused.

The present disclosure is further illustrated by the following examples, but the present disclosure is not limited thereby.

Example 1

In order to eliminate the corrosion of downstream devices caused by the chloride in the reforming raw material, a dechlorination reactor is connected in series after the prehydrogenation reactor, and the hydrogen chloride It reacts with the alkali metal calcium on the dechlorination agent to generate calcium chloride, thereby removing hydrogen chloride in the reforming raw material, and also prevents the phenomenon that hydrogen chloride reacts with ammonia to generate ammonium chloride to block the device. When the chlorine content at the outlet of the dechlorination reactor exceeds 0.5 μg/g, the dechlorination tank is broken, and the dechlorination agent needs to be removed and refilled with fresh dechlorination agent before being put into use. Get 100g of above-mentioned spent dechlorination agent, X-ray fluorescence analysis (XRF) measures the element content in the sample, and composition is shown in Table 1.

The waste dechlorination agent in this example is first calcined under a nitrogen atmosphere to remove the oil gas adsorbed by the waste dechlorination agent to obtain the first material; wherein the conditions for the first roasting include: treatment at a high temperature of 500° C. for 4 hours to reduce to room temperature; take 500 ml of hydrochloric acid solution with an equivalent concentration of 0.5 and place it in a beaker, slowly add the first material for immersion treatment, the immersion time is 4 hours, measure the pH value of the solution concentration, keep the pH value below 3, and then filter , washing to obtain the second material; the second material is subjected to drying treatment and second roasting treatment; wherein the conditions of drying treatment include: drying in a 120°C drying oven for 4 hours, and the conditions of the second roasting treatment include: placing The furnace was roasted at 450° C. for 4 hours and then lowered to room temperature; the acid gas desiccant prepared from the high-temperature dechlorination agent of waste prehydrogenation product prepared in this example was designated as A.

Example 2

Under the normal operating conditions of the reforming unit, the reformed hydrogen contains about 1-3 μg/L hydrogen chloride and a small amount of ammonium chloride, and the reformed hydrogen containing the above-mentioned hydrogen chloride and ammonium chloride gradually It is deposited and accumulated to a certain extent, causing the compressor to be blocked and shut down. At the same time, ammonium chloride is decomposed into hydrochloric acid under the action of condensed water, causing corrosion under the scale. The low-temperature dechlorination process is to string the re-contacted reformed hydrogen into the dechlorination reactor. The dechlorination operation temperature is between 4-40°C, but it is greatly affected by the ambient temperature (temperature of the four seasons). The hydrogen chloride and ammonium chloride in the reformed hydrogen are removed, thereby avoiding the blockage and corrosion of the hydrogen circulation compressor. When the chlorine content at the outlet of the dechlorination reactor exceeds 0.5 μg/L, the dechlorination tank penetrates, and the dechlorination agent It needs to be unloaded and refilled with fresh dechlorination agent before use. Get 100g of above-mentioned waste dechlorination agent, and X-ray fluorescence analysis (XRF) measures the content of elements in the sample, and the composition is shown in Table 2.

Carry out the first roasting of the waste dechlorination agent in this example under a nitrogen atmosphere, remove the oil gas adsorbed by the waste dechlorination agent, and obtain the first material; wherein the conditions of the first roasting include: treatment at a high temperature of 500°C for 4 hours Cool down to room temperature; take 500 ml of hydrochloric acid solution with an equivalent concentration of 0.2 and place it in a beaker, slowly add the first material for impregnation treatment, the impregnation time is 4 hours, measure the pH value of the solution concentration, and keep the pH value below 3 , and then filtered and washed to obtain the second material; the second material is subjected to drying treatment and second roasting treatment; wherein the conditions of the drying treatment include: drying in a 120°C drying oven for 4 hours, and the conditions of the second roasting treatment include: Calcined in a muffle furnace at 450° C. for 4 hours and then lowered to room temperature; the acid gas desiccant prepared from waste reformed hydrogen dechlorination agent prepared in this example is numbered B.

Example 3

The dechlorination technology of regenerative flue gas of reforming unit includes dechlorination of recycled regenerated gas and vented air. Generally, the chloride in the regenerated gas is about 20μg/L to 2500μg/L. In order to eliminate the chloride in the reforming raw material, the downstream Corrosion effect of the device, it is necessary to set up a dechlorination reactor, use the waste heat of the regeneration heat (the temperature is usually between 200-500 ℃), hydrogen chloride and the alkali metal calcium on the dechlorination agent react to generate calcium chloride, so that the regeneration gas Hydrogen chloride removal, when the chlorine content at the outlet of the dechlorination reactor exceeds 0.5 μg/g, the dechlorination tank will break through, and the dechlorination agent needs to be removed and refilled with fresh dechlorination agent before being put into use. Take 100g of the above-mentioned waste dechlorination agent, and X-ray fluorescence analysis (XRF) measures the content of elements in the sample, and the composition is shown in Table 3.

The waste dechlorination agent in this example is first calcined under a nitrogen atmosphere to remove the oil gas adsorbed by the waste dechlorination agent to obtain the first material; wherein the conditions for the first roasting include: treatment at a high temperature of 500° C. for 4 hours to reduce to room temperature; take 500 milliliters of hydrochloric acid solution with an equivalent concentration of 0.5 and place it in a beaker, slowly add the waste dechlorination agent for immersion treatment, the immersion time is 4 hours, measure the pH value of the solution concentration, keep the pH value below 3, and then Filter and wash to obtain the second material; carry out drying treatment and second roasting treatment on the second material; wherein the drying treatment conditions include: drying in a 120°C drying oven for 4 hours, and the second roasting treatment conditions include: placing The furnace was fired at 450°C for 4 hours, and then lowered to room temperature; the acid gas desiccant prepared from waste regeneration gas dechlorination agent prepared in this example was designated as C.

test case 1

Put 100g of the acid gas desiccant obtained in Example 1-3 into a tubular container with ceramic balls at both ends, raise the temperature to 160°C under a dry nitrogen atmosphere, and then feed the acid gas with a flow rate of 1500ml/h. The composition of the acid gas As follows: N ₂ = 88%, CO ₂ = 14%, O ₂ = 2%, H ₂ O = 6%, HCl = 1500μg/L, during the contact process, the water in the gas is combined with the calcium chloride in the desiccant It becomes calcium chloride hydrate, and hydrogen chloride does not react with calcium chloride, so as to remove water from acidic gas and measure the water content in tail gas in real time. When the water content is 50μg/L, the drying process ends, and various drying The water content adsorbed by the agent is shown in Table 4.

Example 4

Take the water-containing desiccant A in Test Example 1 that has been in contact with acidic gas. In a dry nitrogen environment, raise the temperature and control the inlet temperature to 290°C. In the initial stage of regeneration, the outlet temperature is not high due to the evaporation of the adsorbed water. With the increase of time, The outlet temperature will gradually increase as the water content of the desiccant decreases. When the outlet temperature of the drying tank reaches 280°C, the regeneration is over, and the reaction temperature is lowered to 160°C. Switch to the acidic gas containing water in Example 4 and put it into use again. , to achieve drying dehydration - dehydration regeneration recycling.

Comparative example 1

The dehydration process of regenerated flue gas applied to a 700,000-ton/year continuous reforming unit in a refinery: the regenerated flue gas comes out of the catalyst coker, and the hydrogen chloride in the regenerated flue gas is dechlorinated by solid dechlorination at a pressure of 0.6MPa and a temperature of 500°C. Dehydrate to below 0.5μg/L, then reduce the temperature of the regeneration gas to 40°C through heat exchange, contact the desiccant at 40°C to remove the water in the regeneration gas to below 50μg/L, and then heat it up The temperature is increased to 500°C, and returned to the charcoal burner through the circulating compressor, so that it can be recycled, and the regeneration gas is regenerated every 3 days with a desiccant.

Since this drying and dehydration process requires dechlorination, the chlorine loss of the catalyst during the charcoal burning process is relatively large, and it is necessary to supplement the chlorine loss caused by charcoal dechlorination in the oxychlorination step. The chlorine loss is large and the energy consumption is large.

Table 1

Dechlorination agent components Composition m% <![CDATA[Na₂O]]> 0.65 MgO 0.55 <![CDATA[Al₂O₃]]> 8.56 CaO 57.00 Cl 31.68 <![CDATA[Fe₂O₃]]> 1.56

Table 2

Dechlorination agent components Composition m% <![CDATA[Na₂O]]> 1.35 MgO 0.85 <![CDATA[Al₂O₃]]> 59.89 CaO 25.00 Cl 11.68 <![CDATA[Fe₂O₃]]> 1.23

table 3

Table 4

Desiccant number Water absorption, m% A 30 B 16 C 33

The preferred embodiments of the present disclosure have been described in detail above, but the present disclosure is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present disclosure, various simple modifications can be made to the technical solutions of the present disclosure. These simple modifications All belong to the protection scope of the present disclosure.

In addition, it should be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner if there is no contradiction. The combination method will not be described separately.

In addition, various implementations of the present disclosure can be combined arbitrarily, as long as they do not violate the idea of the present disclosure, they should also be regarded as the content disclosed in the present disclosure.

Claims (10)

1. a method for preparing acid gas dry dehydrating agent by waste dechlorination agent, is characterized in that, described method comprises: S1. Carrying out the first roasting treatment on the waste dechlorination agent under an inert atmosphere to obtain the first material; S2. Dip the first material in an acid solution and then filter and wash it to obtain a second material; S3, performing drying treatment and second roasting treatment on the second material; Wherein, the waste dechlorination agent contains calcium oxide and hydroxide, aluminum oxide, sodium oxide, magnesium oxide, ferric oxide and calcium chloride. 2. The method according to claim 1, wherein, based on the total weight of the waste dechlorination agent, the weight percent of the oxide and hydroxide of calcium is 8-70wt%, and the weight percent of aluminum oxide is 30-70wt%. 80wt%, the weight percent of sodium oxide is 0.4-8wt%, the weight percent of magnesium oxide is 0.3-2wt%, the weight percent of ferric oxide is 0.5-2wt%, and the weight percent of calcium chloride is 20-75wt%; Preferably, the weight percent of calcium oxide and hydroxide is 10-65wt%, the weight percent of aluminum oxide is 35-75wt%, the weight percent of sodium oxide is 0.5-5wt%, the weight percent of magnesium oxide is 0.5- 1.5 wt%, the weight percentage of ferric oxide is 1-1.6 wt%, and the weight percentage of calcium chloride is 35-70 wt%. 3. The method according to claim 1, wherein the inert atmosphere is selected from one of a nitrogen atmosphere and an argon atmosphere, preferably a nitrogen atmosphere. 4. The method according to claim 1, wherein the pH value of the acid solution is not more than 3, and the acid solution is selected from hydrochloric acid. 5. The method of claim 1, wherein, In step S1, the conditions of the first calcination treatment include: the temperature is 450-550°C, preferably 480-520°C; the time is 3-6 hours, preferably 4-5 hours; In step S2, the conditions of the dipping treatment include: the temperature is 30-80°C, preferably 50-60°C; the time is 2-5 hours, preferably 3-4 hours; In step S3, the conditions of the drying treatment include: the temperature is 100-130°C, preferably 110-120°C; the time is 2-5 hours, preferably 3-4 hours; the conditions of the second roasting treatment include: The temperature is 400-500°C, preferably 430-450°C; the time is 2-5 hours, preferably 3-4 hours. 6. An acid gas drying and dehydrating agent, characterized in that, the acid gas drying and dehydrating agent is prepared according to the method according to any one of claims 1-5. 7. The acid gas drying and dehydrating agent according to claim 6, wherein the acid gas drying and dehydrating agent contains 35-70% by weight of calcium chloride. 8. The acid gas drying and dehydrating agent according to claim 6, wherein the acid gas drying and dehydrating agent has a particle diameter of 1-5 mm, preferably 2-4 mm; a specific surface area of 30-100 m ² /g, and a total pore size of The volume is 0.15-0.35cc/g. 9. A method for drying and dehydrating an acid gas containing hydrogen chloride, characterized in that, the method for preparing an acid gas drying and dehydrating agent by the waste dechlorination agent described in any one of claims 1-5 with the acid gas The obtained acid gas drying dehydrating agent or the acid gas drying dehydrating agent described in any one of claims 6-8 are contacted and dehydrated; Optionally, the dehydration and drying conditions include: a temperature of 50-200° C., preferably 150-180° C., and a pressure of 0.1-1.0 MPa, preferably 0.3-0.8 MPa. 10. The method according to claim 9, wherein the method further comprises: when the water content in the acid gas passing through the acid gas desiccant is greater than 50 μg/L, regenerating the acid gas drying and dehydrating agent; Optionally, the regeneration conditions include: roasting the acid gas drying dehydrating agent to be produced in a nitrogen atmosphere; optionally, the roasting temperature is 260-310°C.