WO2022042367A1

WO2022042367A1 - System for synthesizing adsorbent of vocs from fly ash and waste grease

Info

Publication number: WO2022042367A1
Application number: PCT/CN2021/112952
Authority: WO
Inventors: 王琪; 李旭; 张兴营; 程阿超; 刘练波; 刘蓉; 邱会哲
Original assignee: 华能国际电力股份有限公司; 中国华能集团清洁能源技术研究院有限公司
Priority date: 2020-08-26
Filing date: 2021-08-17
Publication date: 2022-03-03
Also published as: CN212492970U

Abstract

A system for synthesizing an adsorbent of VOCs from fly ash and waste grease. Using circulating fluidized bed fly ash which is difficult to use by means of conventional technology, and using waste grease at the same time may obtain the adsorbent of VOCs and a compound chemical fertilizer by-products, thereby implementing the use of waste to treat waste. Moreover, the system is environmentally friendly, and the product has a large specific surface area, a good adsorption effect and a low cost.

Description

A system for synthesizing VOCs adsorbent from fly ash and waste oil

This application claims the priority of the Chinese patent application with the application number 202021815250.8 and the invention titled "A system for synthesizing VOCs adsorbents from fly ash and waste oil", which was submitted to the China Patent Office on August 26, 2020, the entire contents of which are Incorporated herein by reference.

technical field

The application belongs to the field of comprehensive utilization of waste, and in particular relates to a system for synthesizing a VOCs adsorbent from fly ash and waste oil.

Background technique

Volatile organic compounds (VOCs) are organic chemicals with high vapor pressure at room temperature, generally referring to organic substances with a boiling point less than 250°C, such as benzene, formaldehyde, ethanol, acetone, etc. There are many kinds of VOCs, mainly from decoration, paint, industrial production, fuel combustion, oil storage and transportation, automobiles, cooking, most of the odors are VOCs. Many VOCs can adversely affect human health, such as irritation to the eyes and respiratory system, causing headaches, nausea, nosebleeds, allergies, memory impairment, fatigue and other symptoms, damage to the liver, kidneys and central nervous system, some of which VOCs are also closely related to cancer. In addition, VOCs are also one of the main pollutants causing air pollution such as haze and photochemical smog.

Common methods for removing VOCs include adsorption method, absorption method, condensation method, catalytic combustion method, biotransformation method, etc. Among them, adsorption method is the most widely used and can remove low-concentration VOCs that are difficult to deal with by other methods. Adsorbents commonly used in adsorption methods include activated carbon, zeolite molecular sieves, and diatomaceous earth. Among them, the price of activated carbon is low, but the safety of regeneration operation is poor, and the performance of regeneration and recovery is poor, so the cost of the whole life cycle is high. Zeolite molecular sieves have high temperature resistance and long life. The molecular sieve adsorption method represented by zeolite runners is widely used in the field of VOCs treatment, but the cost of zeolite molecular sieves is usually high. In recent years, the technology of synthesizing molecular sieves from fly ash has been developed. The synthesis of zeolite molecular sieves from fly ash is expected to reduce the cost of zeolite molecular sieves, and make zeolite molecular sieves with high adsorption, high reproducibility and high regeneration safety economical and large-scale. It is possible to apply to VOCs adsorption.

Fly ash refers to the fine fly ash obtained after the flue gas of coal-fired boilers is collected by the dust collector. In a broad sense, fly ash also includes furnace bottom ash. my country is a big coal country. China consumes half of the world's coal and produces about 500 million tons of fly ash every year. If a large amount of fly ash is simply stored without treatment, it will not only occupy a lot of land, but also cause environmental hazards. Fly ash is mostly used in low value-added fields such as cement, building materials and road construction. Therefore, it is urgent to develop new ways to utilize fly ash and to use fly ash to prepare high value-added products. In recent years, a number of technologies for synthesizing molecular sieves from fly ash have been produced.

Chinese patent CN201710393382.2 applies for a method for preparing VOCs molecular sieve adsorption material with fly ash as raw material. After alkali fusion calcination of fly ash, hydrothermal treatment with structural directing agents such as CTAB is added to obtain a specific surface area of up to 67.52 m ² /g. , but expensive structural directing agents limit the large-scale application of this method.

Chinese patents CN201911057138.4 and CN201911057140.1 propose a method for preparing a modified fly ash adsorbent for VOCs and a new process for treating VOCs with modified fly ash. The modified fly ash adsorbent was obtained by grinding and alkali dissolving at 60℃, and the VOCs were treated by adsorption and high temperature oxidation. However, this technology uses 20% hydrochloric acid solution, which consumes a large amount of acid and generates a relatively large amount of waste liquid. The treatment effect of VOCs gas needs to be further improved.

Waste oil usually refers to waste edible oil, including swill oil produced in catering and food industries, frying waste oil, condensate oil from range hoods, oil that does not meet the use standard produced in oil processing, storage and transportation, and urban sewer oil floating matter, commonly known as gutter. Oil. If waste oils and fats are processed by illegal businesses and then flow into the food market, they will cause serious harm to human health.

The utilization of waste oils and fats has also attracted people's attention. In addition to the conventional soap making technology, researchers have also developed some new applications. CN201410468577.5 proposes a method for preparing polyol from waste oil, which uses a solid acid catalyst with a large hydrophobic surface and has both a sulfonic acid group and a carboxylic acid group to catalyze the esterification and transesterification of waste oil and methanol. Acid-catalyzed epoxidation, ring-opening, and filtration to recover the catalyst, and distillation under reduced pressure to remove water to obtain bio-oil-based polyol. CN201710839683.3 discloses a method for preparing high-purity bio-alkane by using waste oil. The waste oil is dewatered and impurity is removed. Under the action of a modification catalyst, hydrodeoxygenation, denitrification and upgrading are carried out. After oil and water are separated, biomass growth is obtained. Straight chain paraffin oil. CN201310245928.1 discloses a method for preparing acetylene by thermal plasma cracking waste grease. The waste grease is filtered, atomized, mixed with a conveying gas and then entered into a thermal plasma jet of a plasma generator, cracked and quenched in milliseconds After cooling, a cracked gas containing acetylene is obtained. CN201910976259.2 proposes a method for preparing an environmentally friendly plasticizer by using waste oil and its application, using higher fatty acids purified from waste oil, methanol, 50% hydrogen peroxide, trimellitic anhydride and acetic anhydride as the main raw materials. Four-step reaction of oxidation, ring-opening esterification and acetylation is used to prepare acetofatty acid methyl ester-trimellitate, an environmentally friendly plasticizer product. CN201410166050.7 proposes an emulsifier for oil-based drilling fluid, which is used as a component of the emulsifier by reacting waste oil with an alkali to obtain a saponified compound, and reacting with an organic amine under the catalytic condition of an alkali to obtain an amide compound. Although a lot of progress has been made in the utilization of waste oil in recent years, its application in the field of adsorbents, especially VOCs gas adsorbents, has not been reported.

SUMMARY OF THE INVENTION

The purpose of this application is to provide a system for synthesizing VOCs adsorbents from fly ash and waste grease, to overcome the defects of the prior art, the application solves the problem of utilization of fly ash waste and waste grease, and simultaneously treats VOCs air pollution things, use waste to treat waste.

To achieve the above object, the application adopts the following technical solutions:

A system for synthesizing VOCs adsorbents from fly ash and waste grease, comprising an air flow grinder for grinding circulating fluidized bed fly ash, the outlet of the air flow grinder is provided with a grinder hopper, and the outlet of the grinder hopper is connected to a vibrating screen through a vibrating screen. The first stirred tank is connected with a lye pump for transporting potassium hydroxide solution and a buffer pump for transporting urea solution, and the outlet of the first stirred tank is connected to the second stirred tank, and the second stirred tank The outlet is divided into two paths, one is connected to the third stirring tank, the other is connected to the strong stirring mixing tank through the heat exchanger, and the strong stirring mixing tank is connected to the waste oil used for conveying waste oil with a moisture content of <10%. The rotor pump and the apparent viscosity probe for detecting apparent viscosity are conveyed. The outlet of the strong stirring mixing kettle is connected to the colloid mill. The outlet of the colloid mill and the outlet of the third stirring kettle are connected to the high pressure crystallization kettle. A sulfur dioxide gas distributor is connected to the kettle, the outlet of the high-pressure crystallization kettle is connected to a centrifugal filter, the liquid phase outlet of the centrifugal filter is connected to the fourth stirring kettle, and the fourth stirring kettle is connected with a neutralization pump, and the fourth stirring kettle The outlet of the first drying tower is connected to the first drying tower, the outlet of the first drying tower is connected to the compound fertilizer receiving hopper, the solid phase outlet of the centrifugal filter is connected to the emulsification shearing homogenizing kettle, and the emulsification shearing homogenizing kettle is connected with a carrier and a stick. The coagulation conveying pump, the outlet of the emulsification shearing homogenizer is connected to the second drying tower, and the outlet of the second drying tower is connected with a VOCs adsorbent collecting hopper.

Further, a fly ash fine powder belt conveyor is arranged between the vibrating screen and the first stirring tank.

Further, a VOCs adsorbent precursor belt conveyor is arranged between the solid phase outlet of the centrifugal filter and the emulsification shearing homogenizer.

Further, a compound fertilizer packaging machine is connected to the outlet of the compound fertilizer collecting hopper.

Further, the outlet of the VOCs adsorbent collecting hopper is connected with a VOCs adsorbent packaging machine.

Further, the outlet of the first stirring kettle is provided with a first delivery pump, the outlet of the second stirring kettle is provided with a second delivery pump, the outlet of the strong stirring mixing kettle is provided with a third delivery pump, and the outlet of the third stirring kettle is provided with a third delivery pump. There is a fourth delivery pump, and a fifth delivery pump is arranged at the outlet of the high-pressure crystallization kettle.

Further, a first program-controlled valve is arranged between the first delivery pump and the second stirring tank, a second program-controlled valve is arranged between the second delivery pump and the third stirring tank, and the second delivery pump and the heat exchanger are connected. A third program-controlled valve is arranged between the three pumps, a fourth program-controlled valve is arranged between the third delivery pump and the colloid mill, a fifth program-controlled valve is arranged between the fourth delivery pump and the high-pressure crystallization kettle, and the fifth delivery pump and the centrifugal filter A sixth programmable valve is arranged therebetween.

Compared with the prior art, the present application has the following beneficial technical effects:

The present application simultaneously utilizes fly ash waste and waste grease for synthesizing an adsorbent capable of adsorbing air pollutants VOCs, thereby realizing waste treatment with waste. Through the synergistic effect of urea buffer solution and potassium hydroxide, the controllable matching of fly ash alkali dissolution rate, waste oil hydrolysis rate, gel formation rate and micelle conversion rate can be achieved. The coupling effect with the surface modification of the adsorbent can realize the synthesis of high-performance VOCs adsorbent. The synthesized VOCs adsorbent product has a large specific surface area, which can be as high as 230m ² /g, good adsorption effect, and a benzene adsorption capacity of up to 118mg/g. The present application can utilize the high calcium circulating fluidized bed fly ash which is difficult to utilize in the prior art, and solve the utilization outlet of the circulating fluidized bed fly ash. The application can realize continuous production, high production efficiency, green process, environment-friendly, low three waste discharge, and product by-products can be used as fertilizers.

Description of drawings

The accompanying drawings in the description are used to provide further understanding of the application and constitute a part of the application. The schematic embodiments and descriptions of the application are used to explain the application and do not constitute an improper limitation of the application.

FIG. 1 is a schematic structural diagram of the system of the application.

Among them, 1-air flow grinder, 2-grinder hopper, 3-vibrating screen, 4-fly ash fine powder belt conveyor, 5-lye pump, 6-buffer pump, 7-first stirring tank, 8-th A transfer pump, 9- the first program-controlled valve, 10- the second stirring tank, 11- the second transfer pump, 12- the second program-controlled valve, 13- the third stirring tank, 14- the third program-controlled valve, 15- heat exchange device, 16-strong stirring mixing kettle, 17-waste oil conveying rotor pump, 18-strong stirring paddle, 19-apparent viscosity probe, 20-third delivery pump, 21-fourth program-controlled valve, 22-colloid mill, 23- Fourth delivery pump, 24- Fifth program-controlled valve, 25- High pressure crystallization kettle, 26- Sulfur dioxide gas distributor, 27- Fifth transfer pump, 28- Sixth program-controlled valve, 29- Centrifugal filter, 30- Solid phase inlet, 31-liquid phase inlet, 32-neutralization pump, 33-fourth stirring tank, 34-first drying tower, 35-compound fertilizer collecting hopper, 36-compound fertilizer packaging machine, 37-VOCs adsorption Precursor belt conveyor, 38-carrier and binder delivery pump, 39-emulsification shearing homogenizer, 40-second drying tower, 41-VOCs adsorbent collecting hopper, 42-VOCs adsorbent packaging machine.

detailed description

The application is described in further detail below:

A system for synthesizing VOCs adsorbents from fly ash and waste grease, comprising an air flow grinder 1 for grinding circulating fluidized bed fly ash, the outlet of the air flow grinder 1 is provided with a grinder hopper 2, and the outlet of the grinder hopper 2 passes through The vibrating screen 3 is connected to the first stirring tank 7, a fly ash fine powder belt conveyor 4 is arranged between the vibrating screen 3 and the first stirring tank 7, and the first stirring tank 7 is connected with a potassium hydroxide solution for transporting The lye pump 5 and the buffer pump 6 for transporting the urea solution, the outlet of the first stirred tank 7 is connected to the second stirred tank 10, and the outlet of the second stirred tank 10 is divided into two paths, one is connected to the third stirred tank The kettle 13, the other way is connected to the strong stirring and mixing kettle 16 through the heat exchanger 15, and the strong stirring and mixing kettle 16 is connected with a waste grease conveying rotor pump 17 for conveying waste grease with a moisture content of <10% and a detection table. The apparent viscosity probe 19 of the apparent viscosity, the outlet of the strong stirring mixing kettle 16 is connected to the colloid mill 22, the outlet of the colloid mill 2 and the outlet of the third stirring kettle 13 are jointly connected to the high pressure crystallization kettle 25, and the high pressure crystallization kettle 25 The sulphur dioxide gas distributor 26 is connected on it, the outlet of the high-pressure crystallization kettle 25 is connected to the centrifugal filter 29, the liquid phase outlet 31 of the centrifugal filter 29 is connected to the fourth stirred tank 33, and the fourth stirred tank 33 is connected with neutralization. The pump 32, the outlet of the fourth stirring tank 33 is connected to the first drying tower 34, the outlet of the first drying tower 34 is connected to the compound fertilizer receiving hopper 35, and the solid phase outlet 30 of the centrifugal filter 29 is connected to the emulsification shearing homogenizing kettle 39, a VOCs adsorbent precursor belt conveyor 37 is provided between the solid phase outlet 30 of the centrifugal filter 29 and the emulsification shear homogenizer 39, and the emulsification shear homogenizer 39 is connected with a carrier and a binder The outlet of the delivery pump 38, the emulsification shearing homogenizer 39 is connected to the second drying tower 40, the outlet of the second drying tower 40 is connected with a VOCs adsorbent hopper 41, and the outlet of the compound fertilizer collection hopper 35 is connected with compound fertilizer The packaging machine 36, the outlet of the VOCs adsorbent receiving hopper 41 is connected with a VOCs adsorbent packaging machine 42.

The outlet of the first stirring kettle 7 is provided with a first delivery pump 8, the outlet of the second stirring kettle 10 is provided with a second delivery pump 11, the outlet of the strong stirring mixing kettle 16 is provided with a third delivery pump 20, and the third The outlet of the stirring kettle 13 is provided with a fourth delivery pump 23, and the outlet of the high-pressure crystallization kettle 25 is provided with a fifth delivery pump 27; a first program-controlled valve 9 is provided between the first delivery pump 8 and the second stirring kettle 10 , a second program-controlled valve 12 is arranged between the second delivery pump 11 and the third stirring tank 13, a third program-controlled valve 14 is arranged between the second delivery pump 11 and the heat exchanger 15, and the third delivery pump 20 is connected to the colloid mill. A fourth program-controlled valve 21 is arranged between 22, a fifth program-controlled valve 24 is arranged between the fourth delivery pump 23 and the high-pressure crystallization kettle 25, and a sixth program-controlled valve is arranged between the fifth delivery pump 27 and the centrifugal filter 29 28.

When used, include the following steps:

S1: take the circulating fluidized bed fly ash, grind it with an air flow grinder 1, then pass through the grinder hopper 2 to the vibrating screen 3, and obtain the fly ash fine powder sieve precipitate below 60 mesh after screening;

S2: get the potassium hydroxide solution and add the first stirred tank 7 by the lye pump 5, add the urea buffer solution in the first stirred tank 7 by the buffer pump 6, obtain a mixed solution, and the molar concentration of potassium hydroxide in the mixed solution is 0.5～5mol/L, urea and potassium hydroxide mol ratio are 0.01～0.2, then be heated to 60～95 ℃, slowly add the powder in the S1 step through the fly ash fine powder belt conveyor 4 to the first stirring tank 7. The coal ash fine powder is sieved and precipitated, the solid-liquid ratio is 1:5 to 1:20, the feeding process is controlled within 5 to 30 minutes, and then it is transported to the second stirring tank 10 through the first delivery pump 8 and the first program-controlled valve 9. Keep stirring in the second stirring tank 10 for 15 to 90 min to obtain the first solid-liquid mixture;

S3: Take out 5-30% of the first solid-liquid mixture for retention, and transport it to the third stirring tank 13 through the second delivery pump 11 and the second program-controlled valve 12 to become the first solid-liquid mixture A, and the rest as the second solid-liquid mixture liquid mixture B;

S4: transfer the remaining first solid-liquid mixture B to the heat exchanger 15 through the second transfer pump 11 and the third program-controlled valve 14 to quench the temperature to 30-60°C, and then transfer it to the strong stirring mixing kettle 16, where Under the strong stirring action of the strong stirring paddle 18, the waste oil with a moisture content of less than 10% is added through the waste oil conveying rotor pump 17 until the apparent viscosity detected by the apparent viscosity probe 19 (using a rotary apparent viscosity probe) reaches 10-400mPa s, to obtain the second solid-liquid mixture;

S5: The second solid-liquid mixture is transported to the colloid mill 22 for processing through the third delivery pump 20 and the fourth program-controlled valve 21, the colloid mill is turned on for 5-15 minutes, and the mixture is allowed to stand for 10-30 minutes. Repeat "open-standby" three times, obtaining a third solid-liquid mixture;

S6: The remaining first solid-liquid mixture A is mixed with the third solid-liquid mixture through the fourth delivery pump 23 and the fifth program-controlled valve 24, and then transferred to the high-pressure crystallization kettle 25. Crystallization at 120°C for 4-72hrs to obtain the fourth solid-liquid mixture;

S7: continuously feed sulfur dioxide into the fourth solid-liquid mixture for 10 min through the sulfur dioxide gas distributor 26, and lower the temperature to obtain the fifth solid-liquid mixture;

S8: The fifth solid-liquid mixture is transported to the centrifugal filter 29 through the fifth delivery pump 27 and the sixth program-controlled valve 28 for centrifugal separation and washing, and the solid phase material port 30 of the centrifugal filter 29 (using a horizontal centrifugal filter) The discharged solid phase is transported to the emulsification shearing homogenizing kettle 39 through the VOCs adsorbent precursor belt conveyor 37, and the carrier and the binder are transported to the emulsification shearing homogenizing kettle 39 through the carrier and binder delivery pump 38 at the same time, It is co-granulated with the solid phase, then dried in the second drying tower 40, and the VOCs adsorbent is sent to the VOCs adsorbent packaging machine 42 through the VOCs adsorbent receiving hopper 41 for packaging;

The liquid phase discharged from the liquid phase material port 31 of the centrifugal filter 29 is transported to the fourth stirred tank 33, and the neutralization reagent is added to the fourth stirred tank 33 through the neutralization pump 32, and the liquid phase is transported to the fourth stirred tank 33 after neutralization. A drying tower 34 is used for drying, and the compound fertilizer by-products obtained by drying are sent to the compound fertilizer packaging machine 35 through the compound fertilizer receiving hopper 35 for packaging.

In order to clearly illustrate the present application, the present application will be further described in detail below with reference to the embodiments.

Example 1

S1: take the circulating fluidized bed fly ash, grind it with an air flow grinder 1, then pass through the grinder hopper 2 to the vibrating screen 3, and obtain a 100-mesh fly ash fine powder sieve precipitate after screening;

S2: get the potassium hydroxide solution and add the first stirred tank 7 by the lye pump 5, add the urea buffer solution in the first stirred tank 7 by the buffer pump 6, obtain a mixed solution, and the molar concentration of potassium hydroxide in the mixed solution is 2.8mol/L, urea and potassium hydroxide mol ratio are 0.05, then heated to 80 ℃, slowly add the fly ash fine powder sieve in the S1 step through the fly ash fine powder belt conveyor 4 to the first stirring tank 7 Precipitate, the solid-liquid ratio is 1:8.2, and the feeding process is controlled at 15min, then is transported to the second stirred tank 10 by the first delivery pump 8 and the first program-controlled valve 9, and kept stirring in the second stirred tank 10 for 30min to obtain the first solid-liquid mixture;

S3: Take out 10% of the first solid-liquid mixture for retention, and transport it to the third stirring tank 13 through the second delivery pump 11 and the second program-controlled valve 12 to become the first solid-liquid mixture A, and the rest as the second solid-liquid mixture B;

S4: The remaining first solid-liquid mixture B is transported to the heat exchanger 15 through the second transport pump 11 and the third program-controlled valve 14 to quench the temperature to 50°C, and then transported to the strong stirring mixing tank 16, where the strong stirring Under the strong stirring action of the slurry 18, the waste oil with a moisture content of less than 10% is added to the waste oil through the waste oil conveying rotor pump 17 until the apparent viscosity detected by the apparent viscosity probe 19 (using a rotary apparent viscosity probe) reaches 65 mPa·s, and the result is obtained. the second solid-liquid mixture;

S5: The second solid-liquid mixture is transported to the colloid mill 22 for processing through the third delivery pump 20 and the fourth program-controlled valve 21, the colloid mill is turned on for 10 minutes, and the mixture is allowed to stand for 20 minutes. liquid mixture;

S6: The remaining first solid-liquid mixture A is mixed with the third solid-liquid mixture through the fourth delivery pump 23 and the fifth program-controlled valve 24, and then transferred to the high-pressure crystallization kettle 25, maintaining a pressure of 0.15 MPa, and crystallizing at 100 °C 18hr to obtain the fourth solid-liquid mixture;

Example 2

S1: take the circulating fluidized bed fly ash, grind it with an air flow grinder 1, then pass through the grinder hopper 2 to the vibrating screen 3, and obtain a 60-mesh fly ash fine powder sieve precipitate after screening;

S2: get the potassium hydroxide solution and add the first stirred tank 7 by the lye pump 5, add the urea buffer solution in the first stirred tank 7 by the buffer pump 6, obtain a mixed solution, and the molar concentration of potassium hydroxide in the mixed solution is 5mol/L, urea and potassium hydroxide mol ratio are 0.01, be heated to 95 ℃ then, slowly add the fly ash fine powder in the S1 step by the fly ash fine powder belt conveyor 4 in the first stirring tank 7 and sieve analysis. material, the solid-liquid ratio is 1:20, the feeding process is controlled at 5min, and then transported to the second stirred tank 10 by the first delivery pump 8 and the first program-controlled valve 9, and kept stirring in the second stirred tank 10 for 15min to obtain the first a solid-liquid mixture;

S3: Take out 30% of the first solid-liquid mixture for retention, and transport it to the third stirring tank 13 through the second delivery pump 11 and the second program-controlled valve 12 to become the first solid-liquid mixture A, and the rest as the second solid-liquid mixture B;

S4: The remaining first solid-liquid mixture B is transported to the heat exchanger 15 through the second transport pump 11 and the third program-controlled valve 14 to quench the temperature to 60°C, and then transported to the strong stirring mixing tank 16, where the strong stirring Under the strong stirring action of the slurry 18, the waste oil with a moisture content of less than 10% is added to the waste oil through the waste oil conveying rotor pump 17 until the apparent viscosity detected by the apparent viscosity probe 19 (using a rotary apparent viscosity probe) reaches 10 mPa·s. the second solid-liquid mixture;

S5: The second solid-liquid mixture is transported to the colloid mill 22 for processing through the third delivery pump 20 and the fourth program-controlled valve 21, the colloid mill is turned on for 5 minutes, and the mixture is allowed to stand for 10 minutes. liquid mixture;

S6: Mix the remaining first solid-liquid mixture A with the third solid-liquid mixture through the fourth delivery pump 23 and the fifth program-controlled valve 24, and then transfer it to the high-pressure crystallization kettle 25, keep the pressure of 0.1 MPa, and crystallize at 80°C 72hr to obtain the fourth solid-liquid mixture;

S8: The fifth solid-liquid mixture is transported to the centrifugal filter 29 through the fifth delivery pump 27 and the sixth program-controlled valve 28 for centrifugal separation and washing, and the solid phase material port 30 of the centrifugal filter 29 (using a horizontal centrifugal filter) The discharged solid phase is transported to the emulsification shearing homogenizing kettle 39 by the VOCs adsorbent precursor belt conveyor 37, and the carrier and the binder are transported to the emulsification shearing homogenizing kettle 39 through the carrier and binder delivery pump 38 at the same time, It is co-granulated with the solid phase, then dried in the second drying tower 40, and the VOCs adsorbent is sent to the VOCs adsorbent packaging machine 42 through the VOCs adsorbent receiving hopper 41 for packaging;

Example 3

S1: take the circulating fluidized bed fly ash, grind it with the jet grinder 1, then pass the grinder hopper 2 to the vibrating screen 3, and obtain the 200-mesh fly ash fine powder sieve precipitate after screening;

S2: get the potassium hydroxide solution and add the first stirred tank 7 by the lye pump 5, add the urea buffer solution in the first stirred tank 7 by the buffer pump 6, obtain a mixed solution, and the molar concentration of potassium hydroxide in the mixed solution is 0.5mol/L, the molar ratio of urea and potassium hydroxide is 0.2, then heated to 60 ° C, and the fly ash fine powder in the step S1 is slowly added to the first stirring tank 7 through the fly ash fine powder belt conveyor 4. material, the solid-liquid ratio is 1:5, the feeding process is controlled at 30min, and then transported to the second stirred tank 10 by the first delivery pump 8 and the first program-controlled valve 9, and kept stirring in the second stirred tank 10 for 90min to obtain the first a solid-liquid mixture;

S3: Take out 5% of the first solid-liquid mixture for retention, and transport it to the third stirring tank 13 through the second delivery pump 11 and the second program-controlled valve 12 to become the first solid-liquid mixture A, and the rest as the second solid-liquid mixture B;

S4: The remaining first solid-liquid mixture B is transported to the heat exchanger 15 through the second transport pump 11 and the third program-controlled valve 14 to quench the temperature to 30°C, and then transported to the strong stirring mixing tank 16, where the strong stirring Under the strong stirring action of the slurry 18, the waste oil with a moisture content of less than 10% is added to the waste oil through the waste oil conveying rotor pump 17 until the apparent viscosity detected by the apparent viscosity probe 19 (using a rotary apparent viscosity probe) reaches 400 mPa·s. the second solid-liquid mixture;

S5: The second solid-liquid mixture is transported to the colloid mill 22 through the third delivery pump 20 and the fourth program-controlled valve 21 for processing, the colloid mill is turned on for 15 minutes, and the mixture is allowed to stand for 30 minutes. liquid mixture;

S6: Mix the remaining first solid-liquid mixture A with the third solid-liquid mixture through the fourth delivery pump 23 and the fifth program-controlled valve 24, and then transfer it to the high-pressure crystallization kettle 25, keep the pressure of 2.0 MPa, and crystallize at 120°C 4hr to obtain the fourth solid-liquid mixture;

S8: The fifth solid-liquid mixture is transported to the centrifugal filter 29 through the fifth delivery pump 27 and the sixth program-controlled valve 28 for centrifugal separation and washing, and the centrifugal filter 29 (using a horizontal centrifugal filter)

The solid phase discharged from the solid phase material port 30 is transported to the emulsification shearing homogenizing kettle 39 through the VOCs adsorbent precursor belt conveyor 37, and is simultaneously transported to the emulsification shearing homogenizing kettle 39 through the carrier and the binder delivery pump 38. The carrier and the binder are granulated together with the solid phase, then dried in the second drying tower 40, and the VOCs adsorbent is sent to the VOCs adsorbent packaging machine 42 through the VOCs adsorbent collecting hopper 41 for packaging;

The effect of the embodiment: the VOCs adsorbents synthesized in Examples 1, 2, and 3 have higher specific surface areas. The specific surface area of the product of Example 1 is 230 m ² /g, and the specific surface area of the product of Example 2 is 103 m ² /g. , the specific surface area of the product of Example 3 is 110 m ² /g. The VOCs adsorbents synthesized in Examples 1, 2, and 3 all have high adsorption capacity for VOCs. Taking benzene as the model compound, the adsorption capacity of the product of Example 1 is 118 mg/g, and the adsorption capacity of the product of Example 2 is 62 mg/g. , the adsorption capacity of the product of Example 3 is 70 mg/g.

It should be noted that the above is only one of the embodiments of the present application, and equivalent changes made according to the system described in the present application are all included in the protection scope of the present application. Those skilled in the art to which this application pertains can substitute the specific examples described in a similar manner, as long as they do not deviate from the structure of the application or go beyond the scope defined by the claims, they all belong to the protection scope of the application.

Claims

A system for synthesizing VOCs adsorbents from fly ash and waste grease, characterized in that it comprises an air-flow grinder (1) for grinding the circulating fluidized bed fly ash, and a grinder hopper is provided at the outlet of the air-flow grinder (1). (2), the outlet of the grinder hopper (2) is connected to the first stirred tank (7) by the vibrating screen (3), and the first stirred tank (7) is connected with the lye pump (5) for transporting potassium hydroxide solution And the buffer pump (6) for transporting urea solution, the outlet of the first stirred tank (7) is connected to the second stirred tank (10), and the outlet of the second stirred tank (10) is divided into two paths, one is connected to the The third stirring tank (13), the other way is connected to the strong stirring and mixing tank (16) through the heat exchanger (15). The waste grease conveying rotor pump (17) and the apparent viscosity probe (19) for detecting apparent viscosity, the outlet of the strong stirring mixing kettle (16) is connected to the colloid mill (22), the outlet of the colloid mill (2) and the The outlet of the third stirring vessel (13) is commonly connected to the high-pressure crystallization vessel (25), the high-pressure crystallizing vessel (25) is connected with a sulfur dioxide gas distributor (26), and the outlet of the high-pressure crystallizing vessel (25) is connected to the centrifugal The filter (29), the liquid phase outlet (31) of the centrifugal filter (29) is connected to the fourth stirred tank (33), and the fourth stirred tank (33) is connected with a neutralization pump (32), and the fourth stirred tank (33) is connected with the neutralization pump (32). The outlet of (33) is connected to the first drying tower (34), the outlet of the first drying tower (34) is connected to the compound fertilizer collecting hopper (35), and the solid phase outlet (30) of the centrifugal filter (29) is connected to the emulsification hopper (35). The shearing and homogenizing still (39) is connected with a carrier and a binder delivery pump (38) on the emulsification shearing and homogenizing still (39), and the outlet of the emulsification shearing and homogenizing still (39) is connected to the second drying tower (38). 40), the outlet of the second drying tower (40) is connected with a VOCs adsorbent collecting hopper (41).
A system for synthesizing VOCs adsorbent from fly ash and waste oil according to claim 1, characterized in that, fly ash fine powder is arranged between the vibrating screen (3) and the first stirring tank (7). Belt conveyor (4).
A system for synthesizing VOCs adsorbents from fly ash and waste oil according to claim 1, wherein the solid phase outlet (30) of the centrifugal filter (29) and the emulsification shearing homogenizer (39) ) is provided with a VOCs adsorbent precursor belt conveyor (37).
The system for synthesizing VOCs adsorbents from fly ash and waste oil according to claim 1, wherein a compound fertilizer packaging machine (36) is connected to the outlet of the compound fertilizer collecting hopper (35).
A system for synthesizing a VOCs adsorbent from fly ash and waste oil according to claim 1, wherein the outlet of the VOCs adsorbent collecting hopper (41) is connected with a VOCs adsorbent packing machine (42).
A system for synthesizing VOCs adsorbents from fly ash and waste oil according to claim 1, wherein the outlet of the first stirring tank (7) is provided with a first conveying pump (8), and the second stirring tank (7) is provided with a first delivery pump (8). The outlet of 10) is provided with the second delivery pump (11), the outlet of the strong stirring mixing kettle (16) is provided with the third delivery pump (20), and the outlet of the third stirring kettle (13) is provided with the fourth delivery pump ( 23), the outlet of the high pressure crystallization kettle (25) is provided with a fifth delivery pump (27).
The system for synthesizing VOCs adsorbents from fly ash and waste grease according to claim 1, characterized in that a first program control system is arranged between the first delivery pump (8) and the second stirring tank (10). Valve (9), a second program-controlled valve (12) is arranged between the second delivery pump (11) and the third stirring tank (13), and a second program-controlled valve (12) is arranged between the second delivery pump (11) and the heat exchanger (15) The third program-controlled valve (14), the fourth program-controlled valve (21) is arranged between the third delivery pump (20) and the colloid mill (22), and the fourth delivery pump (23) and the high-pressure crystallization kettle (25) A fifth program-controlled valve (24) is provided, and a sixth program-controlled valve (28) is provided between the fifth delivery pump (27) and the centrifugal filter (29).