CN113479877A - Preparation method of spherical activated carbon, product and application thereof - Google Patents

Preparation method of spherical activated carbon, product and application thereof Download PDF

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Publication number
CN113479877A
CN113479877A CN202110679952.0A CN202110679952A CN113479877A CN 113479877 A CN113479877 A CN 113479877A CN 202110679952 A CN202110679952 A CN 202110679952A CN 113479877 A CN113479877 A CN 113479877A
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temperature
activated carbon
carbonization
spherical activated
atmosphere
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常明珠
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Shenzhen Global Greenland New Materials Co ltd
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Shenzhen Global Greenland New Materials Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/30—Active carbon
    • C01B32/312—Preparation
    • C01B32/336—Preparation characterised by gaseous activating agents
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L5/00—Preparation or treatment of foods or foodstuffs, in general; Food or foodstuffs obtained thereby; Materials therefor
    • A23L5/40—Colouring or decolouring of foods
    • A23L5/49—Removing colour by chemical reaction, e.g. bleaching
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K33/00—Medicinal preparations containing inorganic active ingredients
    • A61K33/44—Elemental carbon, e.g. charcoal, carbon black
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K47/00—Medicinal preparations characterised by the non-active ingredients used, e.g. carriers or inert additives; Targeting or modifying agents chemically bound to the active ingredient
    • A61K47/02—Inorganic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
    • B01J20/28016—Particle form
    • B01J20/28019—Spherical, ellipsoidal or cylindrical
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/30—Active carbon
    • C01B32/312—Preparation
    • C01B32/318—Preparation characterised by the starting materials
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23V—INDEXING SCHEME RELATING TO FOODS, FOODSTUFFS OR NON-ALCOHOLIC BEVERAGES AND LACTIC OR PROPIONIC ACID BACTERIA USED IN FOODSTUFFS OR FOOD PREPARATION
    • A23V2002/00—Food compositions, function of food ingredients or processes for food or foodstuffs
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/502—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/40—Aspects relating to the composition of sorbent or filter aid materials
    • B01J2220/48—Sorbents characterised by the starting material used for their preparation
    • B01J2220/4812—Sorbents characterised by the starting material used for their preparation the starting material being of organic character

Abstract

The invention belongs to the technical field of adsorption materials, and particularly relates to a preparation method of spherical activated carbon, a product and application thereof. By using the preparation method of the invention, spherical activated carbon with larger particle size, which can not be prepared in the prior art, can be prepared with good yield and lower cost. Also, the resulting activated carbon has physical or mechanical properties that are not expected by those skilled in the art.

Description

Preparation method of spherical activated carbon, product and application thereof
The application is a divisional application of Chinese invention patent application with application number 201710780469.5 and name of 'preparation method of spherical activated carbon and product and application thereof'.
Technical Field
The invention belongs to the technical field of adsorption materials, and particularly relates to a preparation method of spherical activated carbon, a product and application thereof.
Background
Activated carbon has a wide range of non-specific adsorption properties and is therefore the most widely used adsorbent. Activated carbon is generally obtained by carbonizing a carbon-containing starting compound, preferably such a compound that yields an economically reasonable yield, followed by activation. This is because the weight loss due to the removal of volatile components during carbonization and subsequent burnout during activation is significant.
The properties of the activated carbon produced (e.g. fine or coarse porosity, firmness or friability, etc.) depend on the starting material. Conventional starting materials are coconut shell, charcoal and wood, peat, stone coal, pitch, etc., because of their wide sources, the application value of activated carbon is more enhanced.
However, due to the difference in processes, activated carbon may be used in various forms, such as powdered carbon, flake carbon, granular carbon (Kornkohle), shaped carbon (Formkohle), and spherical activated carbon used since the end of the seventies of the twentieth century.
Spherical activated carbon has numerous advantages over other forms of activated carbon such as powdered carbon, flaked carbon, granular carbon, shaped carbon, etc., which make it useful or even essential for certain applications: it is free flowing, resistant to wear or more accurately to dust, and hard. Spherical activated carbon is highly desirable for, for example, specific application areas because of its particular shape and also because of its high abrasion resistance.
Spherical activated carbon is still today produced mainly by a multistage and very expensive process. The most widely known processes include the production of small spheres from stone coal tar pitch and suitable pitch residues from the petrochemical industry, the oxidation of said pitches to render them infusible, followed by low temperature carbonization and activation. For example, spherical activated carbon can also be made from pitch in a multi-stage process. These multi-stage processes are very expensive and the high cost associated with such spherical activated carbon prevents many applications where spherical activated carbon would otherwise be preferred for its performance.
There are many production processes for spherical activated carbon, for example, a carbon-containing raw material is carbonized and activated, and the preparation of spherical activated carbon is realized by respectively regulating and controlling the processing parameters of each stage. However, there are also a number of drawbacks when using existing processes to make spherical activated carbon. For example, in the prior art, it is difficult to obtain spherical activated carbon with larger particle size and simultaneously obtain satisfactory mechanical and strength characteristics in practical production, and the practical application range is greatly limited. In addition, the prior art is difficult to realize the coordination of parameters such as the particle size, the strength, the pore diameter, the specific surface area and the like of the spherical activated carbon and the adsorption performance of the spherical activated carbon. For this reason, it is required to provide spherical activated carbon which, when having a specific surface area, can have mechanical properties superior to those of the prior art. And the spherical activated carbon can obtain the largest particle size on the premise of avoiding the reduction of the performance. Furthermore, a preparation method of the spherical activated carbon which is more stable and suitable for large-scale production needs to be developed.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a preparation method of spherical activated carbon, which comprises the following steps:
1) carbonizing the spherical polymer;
2) activating the product obtained in step 1).
According to the present invention, in step 1), the polymer may be prepared by mixing a monomer and an initiator to perform a polymerization reaction. By way of example, the polymer may be a homopolymer or a copolymer. Wherein, the homopolymer refers to a polymer prepared by polymerizing one monomer, and the copolymer refers to a polymer prepared by polymerizing two or more monomers.
According to the invention, the monomer can be selected from compounds having 2 to 60 carbon atoms and having at least 1 carbon-carbon double bond, for example compounds having 2 to 20 carbon atoms and having at least 1 carbon-carbon double bond. For example, the monomer may be selected from the following: ethylene, propylene, isopropene, butene, isobutylene, pentene, isopentene, neopentene, hexene, isohexene, neohexene, styrene, methylstyrene, acrylic acid, methacrylic acid, methyl acrylate, methyl methacrylate, butadiene, pentadiene, isoprene, pentadiene, isohexadiene, divinylbenzene, diethylene glycol divinyl ether.
Alternatively, the polymer matrix of the copolymer comprises structural units derived from a first monomer having from 2 to 10 carbon atoms and containing at least one carbon-carbon double bond and structural units derived from a second monomer having from 4 to 15 carbon atoms and containing at least two carbon-carbon double bonds.
Preferably, in the polymer matrix of the copolymer, the structural units derived from the first monomer constitute from 75% to 98%, preferably from 80% to 90%, of the total structural units of the polymer network; the structural units derived from the second monomer constitute from 25% to 2%, preferably from 20% to 10%, of the total structural units of the polymer network.
According to the invention, the first monomer is selected from one or more of styrene, methyl styrene, acrylic acid, methacrylic acid, methyl acrylate, methyl methacrylate and mono-olefin with 2-6 carbon atoms, such as ethylene, propylene, isopropene, butene, isobutene, pentene, isopentene, neopentene, hexene, isohexene, neohexene and the like.
According to the invention, the second monomer is selected from one or more of butadiene, pentadiene, isoprene, pentadiene, isohexadiene, divinylbenzene and diethylene glycol divinyl ether.
According to the invention, the polymerization reaction may be a suspension polymerization reaction; preferably, the polymerization is also carried out in the presence of water, dispersants, dispersion aids.
For example, water: dispersing agent: the weight ratio of the auxiliary dispersing agent is 800-1000: 0.5-3.0: 0.05 to 0.2;
when the polymer is a homopolymer, the monomer: the weight ratio of the initiator may be 1: 0.003 to 0.01.
First monomer, if present: a second monomer: the weight ratio of the initiator can be 0.75-0.98: 0.02-0.25: 0.003 to 0.01.
Preferably, the water, the dispersant and the co-dispersant constitute a water phase, and the monomer of the homopolymer, the first monomer of the copolymer, the second monomer and/or the initiator constitute an oil phase; the weight ratio of the oil phase to the water phase can be 1: 4-6.
According to the present invention, the suspension polymerization reaction may comprise:
adding the components into a reaction kettle, introducing compressed air or nitrogen into the reaction kettle, keeping the pressure in the reaction kettle in a positive pressure state with the gauge pressure less than or equal to 0.5MPa, heating to 70-90 ℃, preserving heat for 2-24 hours, heating to 100-150 ℃, preserving heat for 4-36 hours, then washing with water, drying and screening to obtain the spherical polymer.
In a preferred embodiment, the dispersant is an inorganic dispersant such as a silicate, carbonate or phosphate, or a combination thereof, or an organic dispersant such as polyvinyl alcohol, gelatin, carboxymethyl cellulose or polyacrylate, or a combination thereof.
In a preferred embodiment, the co-dispersant is sodium lauryl sulfate, calcium dodecylbenzenesulfonate, sodium dodecylbenzenesulfonate, calcium petroleum sulfonate, sodium petroleum sulfonate or barium stearate, or a combination thereof.
In a preferred embodiment, the initiator is an organic peroxide compound, an inorganic peroxide compound, or an azo compound, or a combination thereof.
In preferred embodiments, the initiator is a diacyl peroxide, a dioxane peroxide, a peroxyester, azobisisobutyronitrile, or a persulfate, or a combination thereof.
Preferably, the polymerization reaction may also be carried out in the presence of a porogen. The porogen may be selected from paraffin, magnesium sulfate, sodium carbonate, gelatin or glycerol, or a combination thereof.
According to the invention, the spherical polymer has a median particle diameter D50May be 0.2 to 1.5mm, for example 0.5 to 1.3mm, such as 0.7 to 1.0mm, and may in particular be 0.5mm, 0.6mm, 0.7mm, 0.8mm, 0.9mm, 1.0mm, 1.1mm or 1.2 mm.
According to the invention, the polymer may be a sulfonated polymer or a non-sulfonated polymer. When non-sulfonated polymers are used, sulfonation may be performed prior to the carbonization step and/or sulfonation may be performed in situ during carbonization.
By way of example, the unsulfonated polymers may also be prepared according to known methods or commercially available.
The sulfonation can be carried out using starting materials known in the art, for example, by contacting the unsulfonated polymer with a sulfonating agent. The sulfonating agent may be selected from sulfuric acid (e.g., concentrated sulfuric acid), oleum, SO3A mixture of one or more of them.
According to the invention, the total weight ratio of the non-sulfonated spherical polymer to the sulfonating agent may be 3:1 to 1:3, for example 2:1 to 1:2, such as 1:1 to 1: 1.5.
The temperature of the sulfonation step may vary over a wide range.
For example, when sulfonation is carried out prior to the carbonization step, the temperature of the sulfonation step may be 60 to 200 ℃, such as 70 to 180 ℃, for example 80 to 150 ℃;
preferably, the sulfonation step may be carried out while raising the temperature within the above-mentioned temperature range. The rate of temperature rise may be no more than 10 deg.C/min, for example no more than 5 deg.C/min, such as no more than 3 deg.C/min.
The time of the sulfonation step may be from 0.5 to 12 hours, preferably from 1 to 10 hours, such as from 2 to 10 hours.
Preferably, the sulfonation is carried out under an inert gas atmosphere, which may be selected from a mixture of one or more of nitrogen, helium, and argon.
According to the present invention, the carbonization in step 1) may be performed in an inert atmosphere or in a mixed atmosphere of an inert gas and oxygen.
Typically, the temperature of the carbonization may be 100-950 ℃, such as 150-900 ℃, such as 300-850 ℃.
When sulfonation is performed prior to the carbonization step, the starting temperature of the carbonization step may be equal to or higher than the ending temperature of the sulfonation temperature.
Preferably, the carbonization step may be carried out while raising the temperature within the above-mentioned temperature range. The rate of temperature rise may be no more than 10 deg.C/min, for example no more than 5 deg.C/min, such as no more than 3 deg.C/min.
Preferably, the carbonization may be performed sequentially in 2 or more temperature zones, for example, sequentially in 2 to 10 temperature zones. And preferably, the temperatures of the temperature regions are different from each other. Alternatively, carbonization may be carried out at a gradient of increasing temperature.
Preferably, the carbonization may have the same or different temperature rise rates and the same or different holding times in different temperature regions.
Preferably, when carbonization is sequentially performed in 2 or more temperature zones, carbonization is first performed in a first temperature zone, and then carbonization is sequentially performed in a next temperature zone, for example, a second temperature zone; for example, the temperature of the first temperature region may be 100 to 500 ℃, for example, 150 to 450 ℃; the temperature of the second temperature zone may be higher than the first temperature zone, for example 500 to 950 ℃, such as 650 to 950 ℃.
Preferably, the carbonization time is from 30 minutes to 10 hours, for example from 1 to 8 hours, such as from 2 to 6 hours.
Preferably, the inert gas is selected from at least one of nitrogen, helium, argon;
preferably, when the carbonization is performed under a mixed atmosphere of an inert gas and oxygen, the volume percentage of oxygen in the mixed atmosphere is 1 to 5%.
It will be appreciated that if the spherical polymer is subjected to temperatures that allow sulfonation, the spherical polymer may also be sulfonated in situ during carbonization.
According to the present invention, the activation of step 2) may comprise a first activation step and a second activation step.
Preferably, the first activation step is carried out in an atmosphere containing water vapor; the second activation step is carried out in the presence of CO2Is carried out in an atmosphere of (2).
Preferably, the temperature of the first activation treatment is 700-; the time for the first activation step may be from 1 to 24 hours, for example from 5 to 15 hours, such as from 6 to 12 hours.
Preferably, the atmosphere of the first activation step comprises or consists of water vapour, in particular a water vapour/inert gas mixture, preferably a water vapour/nitrogen gas mixture.
Preferably, the volume ratio (flow rate ratio) of the nitrogen to the water vapor is 3:1 or more, for example, 4:1 to 10:1, preferably 4:1 to 8: 1.
According to the invention, the atmosphere of the first activation step may be free of other gases, for example free of carbon oxides (e.g. CO)2) Oxygen and ammonia.
Preferably, the temperature of the second activation step is 700-; the time of the second activation step is 1 to 10 hours, for example 3 to 8 hours.
Preferably, the atmosphere of the second activation step comprises CO2E.g. CO2Or CO2Mixtures with inert gases, e.g. CO2And nitrogen.
Preferably, when the second activating atmosphere comprises nitrogen and CO2In the mixture of (1), nitrogen and CO2The volume ratio (flow rate ratio) of (a) may be 10:1 to 1:10, such as 10:1 to 2:1, for example 8:1 to 4:1, such as 3:1 to 2: 1.
According to the invention, the atmosphere of the second activation step may be free of other gases, for example free of water vapour.
According to the present invention, the temperature rise may use a gradient temperature rise. Alternatively, the temperature may be raised to a certain temperature, and then the temperature may be raised again after the temperature is raised to 1 to 240min, for example, 5 to 150 min.
Preferably, the temperature increase process of the present invention may be continuous or intermittent.
The invention also provides spherical activated carbon which is prepared by the method.
Preferably, the specific surface area B of the spherical activated carbon is less than 1250m2/g。
For example, 600m2/g≤B≤1200m2(ii) in terms of/g. As an example, 700m2/g≤B≤1100m2/g。
According to the invention, the median particle diameter D of the spherical activated carbon50May be 0.2 to 1.5mm, for example 0.5 to 1.3mm, such as 0.7 to 1.2mm, and may in particular be 0.5mm, 0.6mm, 0.7mm, 0.8mm, 0.9mm, 1.0mm, 1.1mm or 1.2 mm.
Preferably, the spherical activated carbon has a median pore diameter of 1 to 4nm, for example 1.5 to 3.8nm, such as 1.8 to 3.8 nm.
According to the invention, the spherical activated carbon may have a compressive strength of 10-300N, for example 40-150N, such as 50-140N, such as 50-130N.
The compressive strength refers to the maximum pressure value that each spherical activated carbon can bear.
The spherical activated carbon may have a cracking rate of less than 10.0%, such as 1.0-10.0%, such as 1.5-6.0%, preferably less than 5.0%, such as 3.0-5.0%.
According to the invention, the bulk density of the spherical activated carbon can be 300-1000g/L, preferably 400-800g/L, such as 450-700 g/L.
According to the invention, the iodine adsorption value of the spherical activated carbon is 400-1100mg/g, preferably 500-1000mg/g, such as 600-950 mg/g.
The invention also provides the application of the spherical activated carbon as an adsorbent.
The spherical activated carbon can be used for adsorbing harmful gases such as CO and H2S、HCl、SO2、NOXOne or more of; alternatively, the spherical activated carbon is used in the food industry, e.g. as a ready and/or decolored food.
The invention also provides application of the spherical activated carbon in preparing medicines.
The invention also provides an adsorbent which comprises the spherical activated carbon.
The invention also provides protective clothing, which comprises the spherical activated carbon.
Advantageous effects
The invention provides a preparation method of spherical activated carbon, a product and application thereof. The inventors have surprisingly found that spherical activated carbon having a relatively large particle diameter, for example, spherical activated carbon of 0.2 to 1.5mm or 0.5 to 1.2mm, can be produced in good yield and at relatively low cost using the production method of the present invention, and even that it is possible to produce spherical activated carbon of 0.7 to 1.1 mm. Further, the activated carbon has excellent physical or mechanical properties, and a significantly reduced cracking rate. And, the activated carbon has excellent adsorption characteristics and can efficiently adsorb harmful gases such as CO and H2S、HCl、SO2、NOXOne or more of; alternatively, the spherical activated carbon is used in the food industry, e.g. as a ready and/or decolored food.
Detailed Description
The preparation method of the present invention will be described in further detail with reference to specific examples. It is to be understood that the following examples are only illustrative and explanatory of the present invention and should not be construed as limiting the scope of the present invention. All the technologies realized based on the above-mentioned contents of the present invention are covered in the protection scope of the present invention.
Apparatus and device
The specific surface areas in the examples were measured by a nitrogen physisorption instrument model Belsorp mini II from microtrac bel corp. The compressive strength was tested by a pressure tester of Shanghai Yihuan Instrument science and technology, Inc.
Example 1
1.1 preparation of spherical Polymer matrices
Adding 18 liters of water into a 50 liter polymerization kettle, heating to 45 ℃, respectively adding 10g of magnesium carbonate, 20g of gelatin and 0.15g of methylene blue under the stirring state, adding an oil phase formed by mixing 3kg of methyl styrene, 1kg of dipentene and 20g of benzoyl peroxide after uniformly stirring, adding 1.0kg of paraffin, sealing the polymerization kettle, introducing clean compressed air into the polymerization kettle, and keeping the gas phase pressure in the kettle at 0.02 MPa. Then, stirring is started, liquid beads in the kettle are adjusted to be proper in particle size, the temperature is increased to 80 ℃, the temperature is kept for 12 hours, the temperature is increased to 100 ℃, the temperature is kept for 20 hours, and 2.35kg of white spherical polymer is obtained through filtering, washing, drying and screening.
1.2 sulfonation and carbonization
Mixing the spherical polymer obtained in the step 1.1 with concentrated sulfuric acid in a mass ratio of 1:1, adding the mixture into an acid-resistant rotary tube furnace, and carrying out the following heating treatment at a heating rate of 5 ℃/min under a nitrogen atmosphere:
heating to 100 ℃, and staying for 120 minutes;
heating to 150 ℃, and staying for 240 minutes;
the following heat treatment was carried out at a heating rate of 4 ℃/min:
heating to 300 ℃, and staying for 120 minutes;
heating to 500 ℃, and staying for 240 minutes;
then heated to 650 ℃ and left for 100 minutes. And cooling to obtain a carbonized product.
1.3 activation
In a rotary tube furnace, the carbonized product obtained in the step 1.2 is heated to 800 ℃ at a speed of 3 ℃/min under a mixed atmosphere of water vapor and nitrogen at a flow rate ratio of 1:4.5(L/min), is left for 360min, is then heated to 950 ℃ at a speed of 3 ℃/min under a mixed atmosphere of carbon dioxide and nitrogen at a flow rate ratio of 1:4(L/min), and is left for 120 min. And (3) reducing the temperature to obtain spherical activated carbon GSC1, wherein the yield is 37 percent based on the polymer. The median particle diameter of the product is 0.75mm, the median pore diameter is 3.50nm, and the specific surface area is 958m2The specific weight percentage of the material is/g, the compressive strength is 79.90N, the bulk density is 470g/L, and the cracking rate is 4.72 percent.
Example 2
2.1 preparation of spherical Polymer matrices
Adding 20 liters of water into a 50 liter polymerization kettle, heating to 40 ℃, respectively adding 10g of calcium carbonate, 20g of polyvinyl alcohol and 0.15g of calcium petroleum sulfonate under the stirring state, stirring uniformly, adding an oil phase formed by mixing 3kg of styrene, 1kg of isoprene and 20g of azobisisobutyronitrile, adding 1.6kg of glycerol, sealing the polymerization kettle, introducing clean compressed air into the polymerization kettle, and keeping the gas phase pressure in the kettle at 0.04 MPa. Then, stirring is started, liquid beads in the kettle are adjusted to be proper in particle size, the temperature is increased to 80 ℃, the temperature is kept for 12 hours, the temperature is increased to 100 ℃, the temperature is kept for 20 hours, and 2.67kg of white spherical polymer is obtained through filtering, washing, drying and screening.
2.2 sulfonation and carbonization
Mixing the spherical polymer obtained in the step 2.1 and SO in a mass ratio of 1:1.53Mixing, then adding the mixture into an acid-resistant rotary tube furnace, and carrying out the following heating treatment at a heating speed of 4 ℃/min under a helium atmosphere:
heating to 80 ℃, and staying for 60 minutes;
heating to 150 ℃, and staying for 300 minutes;
the following heat treatment was performed in a mixed atmosphere of 5% by volume of oxygen at a heating rate of 3 ℃/min:
heating to 200 ℃, and staying for 90 minutes;
heating to 500 ℃, and staying for 320 minutes;
then heated to 600 ℃ and left for 120 minutes. And cooling to obtain a carbonized product.
2.3 activation
Heating the carbonized product obtained in the step 1.2 to 950 ℃ at the speed of 3 ℃/min in a rotary tube furnace under the mixed atmosphere of water vapor and nitrogen at the volume ratio of 1:4, staying for 360min, heating to 950 ℃ at the speed of 4 ℃/min in the mixed atmosphere of carbon dioxide and nitrogen at the flow ratio of 1:3(L/min), and staying for 120 min. And (3) reducing the temperature to obtain spherical activated carbon GSC2, wherein the yield is 39% of the polymer. The median particle diameter of the product is 1.15mm, the median pore diameter is 1.90nm, and the specific surface area is 956m2The specific weight percentage of the material is/g, the compressive strength is 52.76N, the bulk density is 460g/L, and the cracking rate is 4.62%.
Example 3
3.1 preparation of spherical Polymer matrices
Adding 20 liters of water into a 50 liter polymerization kettle, heating to 40 ℃, respectively adding 12g of magnesium carbonate, 25g of sodium carboxymethylcellulose and 0.18g of calcium dodecylbenzene sulfonate under the stirring state, stirring uniformly, adding an oil phase formed by mixing 3.6kg of divinylbenzene, 1.2kg of diethylene glycol divinyl ether and 25g of sodium persulfate, adding 2.2kg of sodium carbonate, sealing the polymerization kettle, introducing clean compressed air into the polymerization kettle, and keeping the pressure of the gas phase in the kettle at 0.05 MPa. Then, stirring is started, liquid beads in the kettle are adjusted to be proper in particle size, the temperature is raised to 90 ℃, the temperature is kept for 9 hours, the temperature is raised to 120 ℃, the temperature is kept for 20 hours, and 3.12kg of white spherical polymer is obtained after filtering, washing, drying and screening.
3.2 sulfonation and carbonization
And (3) adding the polymer obtained in the step (3.1) into a 50-liter reaction kettle, adding 10kg of fuming sulfuric acid with the mass concentration of 105%, heating to 110 ℃, preserving the temperature for 16 hours, slowly dripping water after cooling, pumping out 1/3 liquid after the kettle is full, continuously dripping the water until the sulfuric acid concentration in the kettle is less than 5%, and drying to obtain 4.28kg of polymer microspheres. Subsequently, the polymer microspheres were subjected to a heat treatment at a heating rate of 3 ℃/min under a nitrogen atmosphere as follows:
heating to 120 ℃, and staying for 110 minutes;
heating to 180 ℃, and staying for 250 minutes;
the following heat treatment was performed in a mixed atmosphere of 1% by volume of oxygen at a heating rate of 3 ℃/min:
heating to 250 deg.C, and standing for 360 min;
heating to 450 ℃, and staying for 240 minutes;
then heated to 700 ℃ for 90 minutes. And cooling to obtain a carbonized product.
3.3 activation
In a rotary tube furnace, the carbonized product obtained in the step 1.2 is heated to 800 ℃ at the speed of 3 ℃/min in the mixed atmosphere of water vapor and nitrogen at the volume ratio of 1:7(L/min), is kept for 420min, and is then heated to 950 ℃ at the speed of 4 ℃/min in the mixed atmosphere of carbon dioxide and nitrogen at the flow ratio of 1:7(L/min), and is kept for 200 min. And (3) reducing the temperature to obtain spherical activated carbon GSC3, wherein the yield is 42% based on the polymer. The median particle diameter of the product is 0.90mm, the median pore diameter is 2.95nm, and the specific surface area is 1011m2(ii) a compressive strength of 78.24N,the bulk density is 514g/L, and the cracking rate is 3.32 percent.
Example 4
4.1 preparation of spherical Polymer matrices
Adding 18 liters of water into a 50 liter polymerization kettle, heating to 45 ℃, respectively adding 10g of magnesium carbonate, 20g of gelatin and 0.15g of methylene blue under the stirring state, stirring uniformly, adding an oil phase formed by mixing 3kg of methyl styrene, 1kg of dipentene and 20g of benzoyl peroxide, adding 1.3kg of magnesium sulfate, sealing the polymerization kettle, introducing clean compressed air into the polymerization kettle, and keeping the gas phase pressure in the kettle at 0.02 MPa. Then, stirring is started, liquid beads in the kettle are adjusted to be proper in particle size, the temperature is increased to 80 ℃, the temperature is kept for 12 hours, the temperature is increased to 100 ℃, the temperature is kept for 20 hours, and 2.51kg of white spherical polymer is obtained after filtering, washing, drying and screening.
4.2 sulfonation and carbonization
Mixing the spherical polymer obtained in the step 4.1 with concentrated sulfuric acid in a mass ratio of 1:1.3, adding the mixture into an acid-resistant rotary tube furnace, and carrying out heating treatment at a heating rate of 2 ℃/min under a nitrogen atmosphere as follows:
heating to 60 ℃, and staying for 60 minutes;
heating to 130 ℃, and staying for 100 minutes;
heating to 160 ℃, and staying for 150 minutes;
the following heat treatment was performed in a mixed atmosphere of 3% by volume of oxygen at a heating rate of 3 ℃/min:
heating to 400 ℃, and staying for 240 minutes;
heating to 550 deg.C, and standing for 240min
Then heated to 700 ℃ for 100 minutes. And cooling to obtain a carbonized product.
4.3 activation
Heating the carbonized product obtained in the step 4.2 to 750 ℃ at the speed of 3 ℃/min in a rotary tube furnace in the mixed atmosphere of water vapor and nitrogen at the volume ratio of 1:6.5(L/min), standing for 300min, heating to 980 ℃ at the speed of 2 ℃/min in the mixed atmosphere of carbon dioxide and nitrogen at the flow rate ratio of 1:5.5(L/min), and standing for 300 min. Cooling to obtainTo spherical activated carbon GSC4, the yield was 41% based on polymer. The median particle diameter of the product is 0.55mm, the median pore diameter is 2.19nm, and the specific surface area is 704m2The specific weight percentage of the material is/g, the compressive strength is 124.72N, the bulk density is 675g/L, and the cracking rate is 4.92%.
EXAMPLE 5 measurement of iodine adsorption value
Iodine adsorption values of the spherical activated carbons GSC1-GSC4 prepared in examples 1-4 were measured according to GB/T12496.8-2015 "measurement of iodine adsorption value in test method for Wood activated carbon". The measurement results are shown in table 1.
TABLE 1 iodine adsorption values of spherical activated carbons prepared in examples 1 to 4
Examples Iodine adsorption number (mg/g)
Example 1 800
Example 2 780
Example 3 950
Example 4 600
The embodiments of the present invention have been described above. However, the present invention is not limited to the above embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. A preparation method of spherical activated carbon comprises the following steps:
1) carbonizing the spherical polymer;
the carbonization temperature is 100-950 ℃, and the temperature rise speed in the carbonization step is not more than 10 ℃/min, for example not more than 5 ℃/min, such as not more than 3 ℃/min;
2) activating the product obtained in step 1).
2. The production method according to claim 1, wherein the carbonization in step 1) may be performed in an inert atmosphere or in a mixed atmosphere of an inert gas and oxygen;
preferably, the temperature of the carbonization can be 150-900 ℃, such as 300-850 ℃;
preferably, the carbonization may be performed sequentially in 2 or more temperature zones, for example, sequentially in 2 to 10 temperature zones;
preferably, the temperatures of the temperature zones are different from each other, or carbonization may be performed at a temperature of a gradient rise.
3. The production method according to claim 1 or 2, characterized in that, when carbonization is sequentially performed in 2 or more temperature zones, carbonization is first performed in a first temperature zone, and then carbonization is sequentially performed in a next temperature zone, for example, a second temperature zone;
for example, the temperature of the first temperature region may be 100 to 500 ℃, for example, 150 to 450 ℃; the temperature of the second temperature zone may be higher than the first temperature zone, for example 500 to 950 ℃, such as 650 to 950 ℃.
4. The production method according to any one of claims 1 to 3, wherein the activation of step 2) may include a first activation step and a second activation step;
preferably, the temperature of the first activation treatment may be 700-;
preferably, the atmosphere of the first activation step comprises or consists of water vapour, in particular a water vapour/inert gas mixture, preferably a water vapour/nitrogen gas mixture.
5. The production method according to claim 4,
the atmosphere of said first activation step comprises or consists of water vapor, in particular a mixture of water vapor and an inert gas, preferably a mixture of water vapor and nitrogen;
preferably, the volume ratio (flow rate ratio) of the nitrogen to the water vapor is 3:1 or more, for example, 4:1 to 10:1, preferably 4:1 to 8: 1;
according to the invention, the atmosphere of the first activation step may be free of other gases, for example free of carbon oxides (e.g. CO)2) Oxygen and ammonia.
6. The production method according to claim 4 or 5,
the temperature of the second activation step is 700-1300 ℃, preferably 800-1200 ℃, for example 850-950 ℃; the time of the second activation step is 1 to 10 hours, for example 3 to 8 hours;
preferably, the atmosphere of the second activation step comprises CO2E.g. CO2Or CO2Mixtures with inert gases, e.g. CO2A mixture with nitrogen;
preferably, when the second activating atmosphere comprises nitrogen and CO2In the mixture of (1), nitrogen and CO2The volume ratio (flow rate ratio) of (a) may be 10:1 to 1:10, such as 10:1 to 2:1, for example 8:1 to 4:1, such as 3:1 to 2: 1;
preferably, the atmosphere of the second activation step may be free of other gases, for example free of water vapour.
7. The production method according to any one of claims 1 to 6, wherein the polymer may be a homopolymer or a copolymer;
preferably, the polymer may be a sulfonated polymer or a non-sulfonated polymer;
when non-sulfonated polymers are used, sulfonation may be performed prior to the carbonization step and/or in situ during carbonization;
for example, the sulfonating agent may be selected from sulfuric acid (e.g., concentrated sulfuric acid), oleum, SO3A mixture of one or more of;
for example, the total weight ratio of the non-sulfonated spherical polymer to the sulfonating agent can be 3:1 to 1:3, such as 2:1 to 1:2, e.g., 1:1 to 1: 1.5;
when sulfonation is carried out prior to the carbonization step, the temperature of the sulfonation step may be 60 to 200 deg.C, such as 70 to 180 deg.C, for example 80 to 150 deg.C.
8. The method of any one of claims 1-7, wherein when sulfonation is performed prior to the carbonization step, the temperature of the sulfonation step may be 60-200 ℃, such as 70-180 ℃, for example 80-150 ℃;
when sulfonation is performed prior to the carbonization step, the starting temperature of the carbonization step may be equal to or higher than the ending temperature of the sulfonation temperature.
9. Spherical activated carbon produced by the production method according to any one of claims 1 to 7;
preferably, the specific surface area B of the activated carbon is less than 1250m2G, e.g. 600m2/g≤B≤1200m2(ii)/g; for example 700m2/g≤B≤1100m2/g；
Preferably, the spherical activated carbon has a median particle diameter D50May be 0.2-1.5mm, for example 0.5-1.3mm, such as 0.7-1.2 mm;
preferably, the spherical activated carbon has a median pore diameter of 1 to 4nm, for example 1.5 to 3.8nm, such as 1.8 to 3.8 nm;
preferably, the spherical activated carbon may have a compressive strength of 10-300N, for example 40-150N, such as 50-140N, such as 50-130N;
preferably, the spherical activated carbon has a cracking rate of less than 10.0%, such as 1.0-10.0%, such as 1.5-6.0%, preferably less than 5.0%, such as 3.0-5.0%.
10. Use of the spherical activated carbon according to claim 9 as an adsorbent;
preferably, the spherical activated carbon is used for adsorbing harmful gases such as CO, H2S、HCl、SO2、NOXOne or more of;
preferably, the spherical activated carbon is used in the food industry, such as for preparing and/or decolorizing food products.
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