阅读说明：本技术 纸浆模塑品的制造方法及制备系统 (Method and system for producing pulp molded product ) 是由 牛金虎 徐县委 王业连 姜先亮 于 2019-10-21 设计创作，主要内容包括：一种纸浆模塑品的制造方法,包括：碎浆,将相对于总浆板质量比为55-65％的甘蔗浆板和相对于总浆板质量比为45-35％的芦苇浆板与水,进行混合碎浆制得浆料,所述浆料浓度为4.5％-6.0％,甘蔗浆板和芦苇浆板的总质量为总浆板质量；磨浆,对所述浆料进行精磨,且打浆度控制在25～30°SR；稀释,加水稀释至所述浆料浓度为0.2％～0.3％；热压成型,将稀释后的所述浆料通过热压成型制得所述纸浆模塑品。本发明还提出一种上述纸浆模塑品的制备系统。(A method of manufacturing a pulp molded product, comprising: pulping, namely mixing and pulping a sugarcane pulp plate with the mass ratio of 55-65% relative to the total pulp plate, a reed pulp plate with the mass ratio of 45-35% relative to the total pulp plate and water to obtain pulp, wherein the concentration of the pulp is 4.5-6.0%, and the total mass of the sugarcane pulp plate and the reed pulp plate is the mass of the total pulp plate; grinding the pulp, namely finely grinding the pulp, wherein the beating degree is controlled to be 25-30 DEG SR; diluting, namely adding water to dilute until the concentration of the slurry is 0.2-0.3%; and (3) performing hot press molding, namely performing hot press molding on the diluted slurry to obtain the pulp molding product. The invention also provides a preparation system of the pulp molding.)

1. A method of manufacturing a pulp molded product, comprising:

pulping, namely mixing and pulping a sugarcane pulp plate with the mass ratio of 55-65% relative to the total pulp plate, a reed pulp plate with the mass ratio of 45-35% relative to the total pulp plate and water to obtain pulp, wherein the concentration of the pulp is 4.5-6.0%, and the total mass of the sugarcane pulp plate and the reed pulp plate is the mass of the total pulp plate;

grinding the pulp, namely finely grinding the pulp, wherein the beating degree is controlled to be 25-30 DEG SR;

diluting, namely adding water to dilute until the concentration of the slurry is 0.2-0.3%;

and (3) performing hot press molding, namely performing hot press molding on the diluted slurry to obtain the pulp molding product.

2. The production process according to claim 1, wherein, in the pulp crushing, a fluorescent whitening agent, a blue dye and a violet dye are added to the pulp; the fluorescent whitening agent is a bis (triazinylamino) fluorescent whitening agent, the blue dye is an azo metal complex dye, and the violet dye is carbazole dioxazine violet.

3. The method of claim 1, wherein a wet strength agent solution and a dry strength agent solution are added to the pulp after pulping before refining, wherein the volume ratio of the wet strength agent solution to the total pulp is 1.0-2.0%, the volume ratio of the dry strength agent solution to the total pulp is 0.3-0.7%, and the pulp containing the added wet strength agent solution and the dry strength agent solution is the total pulp.

4. The process according to claim 3, wherein the wet strength agent solution is a polyamide polyamine epichlorohydrin and the dry strength agent solution is an acrylamide resin.

5. The method according to claim 1, wherein a sizing agent is added to the stock at the time of dilution, the sizing agent being an alkyl ketene dimer, the volume ratio of the sizing agent to the total stock being 1.0 to 2.0%.

6. The method of claim 1, wherein the pulp is cleaned of impurities after pulping and before refining; dispersing and defibering the pulp after pulping and before dilution; and deslagging the slurry after dilution and before hot-pressing forming.

7. A production system for producing a pulp molded product by the production method according to any one of claims 1 to 6, comprising:

the pulper is used for mixing and pulping the pulp board and water to prepare pulp;

the refiner is connected with the pulper and is used for refining the pulp;

the pulp distribution barrel is connected with the refiner and is used for diluting the refined pulp;

and the hot-press forming machine is connected with the pulp mixing barrel and is used for hot-press forming the pulp molding product by the diluted pulp.

8. The preparation system of claim 7, further comprising:

the slag remover is connected with the pulper and the refiner and is used for removing impurities from the pulp prepared by the pulper, and the refiner is used for finely grinding the pulp which is removed by the impurities from the pulper;

the defibering machine is connected with the refiner and the pulp distribution barrel and is used for dispersing and defibering the pulp refined by the refiner, and the pulp distribution barrel is used for diluting the pulp subjected to dispersion and defibering by the refiner;

and the vortex slag remover is connected with the slurry mixing barrel and the hot-press forming machine and is used for removing slag from the slurry diluted by the slurry mixing barrel, and the hot-press forming machine is used for hot-press forming the slurry subjected to slag removal by the slurry mixing barrel.

9. The preparation system of claim 8, further comprising: and the vibrating screen is connected with the fluffer and the refiner and is used for screening out undissociated slurry dispersed and fluffed by the fluffer and then entering the refiner again for fine grinding.

10. The preparation system of claim 7, further comprising: and the medicament barrel is connected with the pulper and is used for adding a fluorescent whitening agent, a blue dye and a purple dye into the pulper.

Technical Field

The invention relates to the field of paper pulp molded products, in particular to a manufacturing method and a manufacturing system of a paper pulp molded product.

Background

The paper pulp molding product is environment-friendly, high in quality and low in price, and is widely applied to the field of packaging materials. The prior common paper pulp molding product has rough surface, slightly insufficient appearance, poor visual sense and slightly insufficient buffer inner support as a high-end packing box.

Disclosure of Invention

In view of the above, it is necessary to provide a method and a system for producing a pulp molded product to solve the above problems.

A method of manufacturing a pulp molded product, comprising:

pulping, namely mixing and pulping a sugarcane pulp plate with the mass ratio of 55-65% relative to the total pulp plate, a reed pulp plate with the mass ratio of 45-35% relative to the total pulp plate and water to obtain pulp, wherein the concentration of the pulp is 4.5-6.0%, and the total mass of the sugarcane pulp plate and the reed pulp plate is the mass of the total pulp plate;

grinding the pulp, namely finely grinding the pulp, wherein the beating degree is controlled to be 25-30 DEG SR;

diluting, namely adding water to dilute until the concentration of the slurry is 0.2-0.3%;

and (3) performing hot press molding, namely performing hot press molding on the diluted slurry to obtain the pulp molding product.

A manufacturing system for manufacturing a pulp molded product by the above manufacturing method comprises:

the pulper is used for mixing and pulping the pulp board and water to prepare pulp;

the refiner is connected with the pulper and is used for refining the pulp;

the pulp distribution barrel is connected with the refiner and is used for diluting the refined pulp;

and the hot-press forming machine is connected with the pulp mixing barrel and is used for hot-press forming the pulp molding product by the diluted pulp.

According to the manufacturing method and the manufacturing system of the paper pulp molded product, the sugarcane pulp board and the reed pulp board are mixed and pulped in proportion, and the pulping degree of pulp and the concentration of the diluted pulp during pulping are controlled, so that the paper pulp molded product formed by hot pressing has a smooth surface, few burrs and soft visual sense.

Drawings

Fig. 1 is a schematic view of a pulp molded product production system in one embodiment of the present invention.

Fig. 2 is a flow chart of a method of manufacturing the manufacturing system of fig. 1.

Description of the main elements

The following detailed description will further illustrate the invention in conjunction with the above-described figures.

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

It will be understood that when an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. When an element is referred to as being "disposed on" another element, it can be directly on the other element or intervening elements may also be present.

Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used in the description of the invention herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.

Referring to fig. 1 and 2, the present invention provides a method for manufacturing a pulp molded product. Which comprises the following steps:

and step S1, pulping, namely mixing the sugarcane pulp board and the reed pulp board with water and pulping to obtain pulp according to the mass ratio of the sugarcane pulp board to the total pulp board (the sugarcane pulp board and the reed pulp board, the same below) of 55-65% and the mass ratio of the reed pulp board to the total pulp board of 45-35%, wherein the pulp concentration (the ratio of the absolute dry mass of substances filtered out from the pulp (the total dry mass of the pulp board) to the mass of the unfiltered pulp, expressed by mass percentage, the same below) is 4.5-6.0%.

Specifically, a batch feeder 1 and a pulper 2 are provided, and a sugar cane pulp sheet and a reed pulp sheet are fed into the pulper 2 through the batch feeder 1. Water is added into the pulper 2, and the sugarcane pulp board and the reed pulp board are mixed with the water and are disintegrated to prepare pulp.

Wherein, the mass ratio of the sugarcane pulp board to the total pulp board in the pulp boards put into the batch feeder 1 is 55-65%, and the mass ratio of the reed pulp board to the total pulp board is 45-35%. The water content of the sugarcane pulp board and the reed pulp board is lower than 12%. The whiteness of the sugarcane pulp board is more than 65%. The whiteness of the reed pulp board is more than 60 percent. The water added into the pulper 2 is deionized water, and the temperature is above 30 ℃. A flow meter and a concentration meter are arranged in the pulper 2 and are used for controlling the concentration of the pulp to be 4.5-6.0%. The pulper 2 is also internally provided with a heater and a thermometer for controlling the temperature of the pulp to be above 30 ℃.

When pulping, the reed pulp board is mixed with water by the batch feeder 1, and after 7-9 minutes of pulping, the sugarcane pulp board is added, and pulping is continued for 11-13 minutes until the pulping is uniform.

In one embodiment, a cartridge 20 is also provided in communication with the pulper 2. The agent tank 20 is used to add fluorescent whitening agent, blue dye and violet dye to the pulper 2.

The fluorescent whitening agent, the blue dye and the purple dye are respectively added into corresponding auxiliary agents, and then the auxiliary agents added with the fluorescent whitening agent, the blue dye or the purple dye are respectively added into the pulper 2 through the agent barrel 20. In one embodiment, the auxiliary agent is a mixture of propylene glycol, nonionic surfactant and emulsifier, wherein the nonionic surfactant is one or more of alkylphenol ethoxylates (APEO), peregal O and fatty acid methyl ester polyoxyethylene ether (FMEE), the emulsifier is one or a mixture of nonylphenol polyoxyethylene ether emulsifier and polyacrylamide emulsifier, the ratio of the propylene glycol, the nonionic surfactant and the emulsifier is 0.1-1:1-10:1-5, preferably, the ratio of the propylene glycol, the nonionic surfactant and the emulsifier is 0.1-0.2:2:1, the nonionic surfactant can increase the activity of the blue dye and the purple dye and improve the dispersion degree of the blue dye and the purple dye, the propylene glycol is micromolecular polyhydric alcohol and can better improve the mutual compatibility of the components, the emulsifier molecules can be diffused into the blue dye and the purple dye and fixed on the blue dye molecules and the purple dye molecules, so that the dispersibility is improved.

After the sugarcane pulp board is added, the fluorescent whitening agent, the blue dye and the purple dye are respectively added into the pulper 2 through a medicament barrel 20 at 12-18 minutes after pulping, the adding sequence is not limited, and the adding interval of each reagent is 85-95 seconds.

The fluorescent whitening agent is added for the purpose of improving the brightness of the pulp molding and making it bright and pleasant. In one embodiment, the optical brightener is a bis (triazinylamino) type optical brightener VBL (Invitrogen name: C.I. Fluorogenic brightener 151(9CI), CAS No.: 12224-16-7).

The visual whiteness of the paper in the violet-white or blue-white phase is much higher than that in the yellow-white phase. Thus, blue and violet dyes are added to tone the pulp moldings to which the optical brightener is added. In one embodiment, the blue dye is an azo metal complex dye, and is commercially available, no special requirement is imposed on the metal element complexed by the blue dye, such as iron, copper or zinc, the number of azo groups is also not required, and the blue dye can be monoazo, disazo or polyazo, as long as the blue azo complex dye is adopted, the azo metal complex dye can provide certain complexing force, improve the complexing degree and increase the dispersing and suspending effects, the metal complex structure in the azo metal complex dye can adsorb a fluorescent whitening agent in slurry, and the dispersibility and the fluidity are better improved by matching with the use of an auxiliary agent, and meanwhile, the long-chain structure of cellulose is dispersed in each component and reagent; the violet dye is carbazole dioxazine violet, and is commercially available.

And step S2, removing slag and removing impurities from the obtained slurry.

Specifically, a slag remover 3 connected with the pulper 2 and a first pulp barrel 4 connected with the slag remover 3 are provided, pulp obtained by the pulper 2 is injected into the slag remover 3 through a pipeline, impurities (large pulp plates, stone iron wires and other impurities) are removed, the pulp is injected into the first pulp barrel 4 through the pipeline, and the pulp after slag removal is collected.

In one embodiment, the wet strength agent solution and the dry strength agent solution are added to the slurry in the first vat 4 through a reagent vat connected to the first vat 4. The wet strength agent solution is added into the pulp of the first pulp bucket 4, and the dry strength agent solution is added after the interval of 55-65 seconds.

The main purpose of adding the wet strength agent and the dry strength agent is to control the tensile strength and the bursting resistance of the paper pulp molding after cutting. The tensile strength of the pulp molding is 0.845kN/m without adding wet strength agent and dry strength agent²～1.523kN/m²The bursting resistance is 80KPa to 110 KPa; after the wet strength agent and the dry strength agent are added, the tensile resistance is improved to 2.563kN/m²～3.451kN/m²The bursting strength is improved to 150 KPa-190 KPa.

Wherein the volume ratio of the wet strength agent solution to the total pulp (pulp containing the wet strength agent solution and the dry strength agent solution) (the volume ratio of the wet strength agent solution added to the pulp to the total volume of the pulp, expressed as volume percentage, the same applies hereinafter) is 1.0-2.0%, and the volume ratio of the dry strength agent solution to the total pulp is 0.3-0.7%. In one embodiment, the wet strength agent is a commercially available polyamide polyamine epichlorohydrin wet strength agent, and the dry strength agent is an acrylamide resin.

And step S3, refining the pulp obtained in the step S2, and controlling the beating degree (beating degree) of the pulp to be 25-30 degrees SR (Shore).

Specifically, a refiner 5 connected to a first pulp barrel 4 and a second pulp barrel 6 connected to the refiner 5 are provided, and the pulp in the first pulp barrel 4 is injected into the refiner 5 through a pipe to be refined, and is injected into the second pulp barrel 6 through a pipe to be collected after being refined. In the initial stage of refining, the refined pulp flows back to the first pulp barrel 4 to stabilize the beating degree of the pulp.

Wherein, the fine grinding degree of the refiner 5 is controlled, the beating degree of the pulp flowing into the second pulp barrel 6 is controlled to be 25-30 DEG SR, and the concentration of the pulp is controlled to be 4.5-6.0%.

In an embodiment the refiner 5 is a conical disc refiner.

And step S4, defibering, namely dispersing and defibering the fine-ground pulp to remove undissociated pulp.

The defibering is to perform the functions of extrusion, impact, friction, kneading and the like on the fibers in the pulp, so that a plurality of fiber bundles bonded together in the pulp are dispersed into single fibers, and the product uniformity and the surface smoothness are favorably improved.

Specifically, a fluffer 7 connected to the second pulp barrel 6 and a shaker 8 connected to the fluffer 7 are provided, the pulp in the second pulp barrel 6 is injected into the fluffer 7 through a pipe to be dispersed and fluffed, the fluffed undissociated pulp is injected into the shaker 8 through a pipe, and the undissociated pulp is injected into the first pulp barrel 4 again through a pipe by the shaker 8 to be refined again by the refiner 5.

In one embodiment, the fluffer 7 is a cylindrical fluffer, and the sieving machine 8 is a double-layer sieving machine.

And step S5, diluting the slurry obtained in the step S4, and adding water to dilute the slurry until the concentration of the slurry is 0.2-0.3%.

When the concentration of the pulp is 4.5-6.0%, the fibers in the pulp cannot be uniformly dispersed due to the excessively high concentration of the pulp, and impurities in the fibers are difficult to remove, so that the pulp needs to be diluted by water to form a good dispersion in a low-concentration state, and the purification and screening are facilitated.

Specifically, a pulp mixing barrel 9 connected with the fluffer 7 and a third pulp mixing barrel 10 connected with the pulp mixing barrel 9 are provided, the pulp obtained by the fluffer 7 is injected into the pulp mixing barrel 9 through a pipeline, water is added into the pulp mixing barrel 9 for dilution, the diluted pulp is injected into the third pulp mixing barrel 10 through a pipeline, and the diluted pulp is collected.

Wherein, the water added in the slurry preparation barrel 9 is deionized water. When the water temperature is too low, the viscosity of the fibers in the slurry is high, the fluidity is poor, and the demolding is difficult in the subsequent hot press molding, so that the temperature is above 30 ℃. A flow meter and a concentration meter are arranged in the pulp mixing barrel 9 and the third pulp barrel 10 and are used for controlling the pulp concentration to be 0.2-0.3%. The slurry preparation barrel 9 and the third slurry barrel 10 are also internally provided with a heater and a thermometer for controlling the temperature of the slurry to be above 30 ℃.

In one embodiment, a medicament barrel 21 connected to the slurry preparation barrel 9 is also provided. The chemical tank 21 is used for adding a sizing agent to the size preparing tank 9.

The sizing agent is an alkyl ketene dimer, has fluid diffusion and permeation resistance and has a reactive ketone group. After the sizing agent is added into the diluted pulp, the hydroxyl group of the pulp cellulose and the ketone group are subjected to esterification reaction to form covalent bond, a stable film is formed on the surface of the fiber, at the moment, the hydrophobic group (long chain alkyl) is turned to the surface of the fiber, the outer side of the surface is oriented to the hydrophobic group, and the obtained pulp molding product has hydrophobicity and fluid permeation resistance. After the sizing agent is added, the moisture content of the paper pulp molding product after cutting is reduced to 6-8% under the humidity of 60-80%, and the water absorption deformation of the paper pulp molding product is reduced. The sizing agent is added mainly for controlling the water absorption deformation rate of the paper pulp molding after cutting. When no sizing agent is added, the moisture content of the paper pulp molding product after cutting is 15-18% under the humidity of 60-80%. After the slurry in the slurry preparation barrel 9 is diluted for 55-65 seconds, the sizing agent is added into the slurry preparation barrel 9 through the medicament barrel 21.

Wherein the volume ratio of the added sizing agent to the total sizing agent is 1.0-2.0%.

And step S6, deslagging, namely performing vortex deslagging on the slurry obtained in the step S5.

Specifically, a vortex cleaner 11 connected with the third pulp barrel 10 is provided, and the pulp obtained from the third pulp barrel 10 is injected into the vortex cleaner 11 through a pipeline for vortex cleaning to remove fine fibers in the pulp.

In one embodiment, the vortex cleaner 11 is a two-stage cone vortex cleaner.

And step S7, performing hot press molding, namely performing hot press molding dehydration on the slurry obtained in the step S6 after extrusion molding.

Specifically, a hot-press forming machine 12 connected with the vortex deslagging device 11 is provided, slurry obtained by the vortex deslagging device 11 is sucked into the hot-press forming machine 12, extrusion forming dehydration is carried out, and hot-press forming dehydration is carried out through hot-press shaping, so that a paper pulp molding product is obtained.

In one embodiment, the slurry suction mold of the thermoforming machine 12 is perforated and covered with a double-layer net for slurry suction. The mesh surface of the double-layer mesh adopts 150 meshes and 100 meshes in combination.

In one embodiment, the thermoforming machine 12 dehydrates the slurry by an air compressor 13 connected to the thermoforming machine 12.

In one embodiment, the thermoforming machine 12 is a three-stage thermoforming machine, and the pulp molded product is obtained by performing one-time extrusion molding, two-time hot-pressing dehydration, and finally three-time hot-pressing molding.

The three-section type hot-press forming machine comprises a pulp suction forming mechanism, a first hot-press forming mechanism and a second hot-press forming mechanism, wherein the pulp suction forming mechanism is used for sucking pulp and extruding the pulp into a wet blank, the first hot-press forming mechanism is used for performing hot-press dehydration on the wet blank to form a rough blank, and the second hot-press forming mechanism is used for performing hot-press forming on the rough blank again to form the pulp molding product.

Specifically, after the pulp absorption forming mechanism absorbs pulp for 1-10s, extrusion forming is carried out for 20-30s for dewatering, the temperature is controlled to be 90-100 ℃, the moisture content of the pulp absorption obtained material is 55% -60%, and the pulp absorption forming mechanism absorbs pulp for more than 1s again to enable the pulp absorption obtained material to reach the required weight; the pulp suction forming mechanism performs back blowing (blowing towards the first hot pressing forming mechanism) for 0.3-1s, the air pressure value is 0.5-1.0bar, the air suction vacuum value of the first hot pressing forming mechanism is-0.6 to-1 bar, and pulp suction obtained objects are transferred; the first hot-pressing forming mechanism carries out hot pressing on the pulp absorbing obtained object for 10-25s to dehydrate and form a primary hot-pressing product, the temperature is controlled at 110 ℃, and the water content of the primary hot-pressing product is 35-40%; the first hot-pressing forming mechanism performs back blowing (blowing towards the second hot-pressing forming mechanism) for 0.3-1s, the air pressure value is 0.5-1.0bar, the air suction vacuum value of the second hot-pressing forming mechanism is-0.6 to-0.8 bar, and the first hot-pressing product transfer is performed; the second hot-pressing forming mechanism carries out hot-pressing forming on the primary hot-pressed product for 40-45s to obtain the pulp molding product, the temperature is controlled at 130-; the second hot-press forming mechanism performs back blowing (blowing towards an external receiving mechanism) for 0.3-1s, the air pressure value is 0.5-1.0bar, and the external receiving mechanism transfers the obtained paper pulp molding product through the suction vacuum value of-0.6 to-1 bar, thereby completing the hot-press forming.

Compared with a two-section type hot-press forming machine, the three-section type hot-press forming machine can effectively avoid the deformation phenomenon of the paper pulp molded product caused by one-section type hot-press forming by performing hot-press forming on a rough blank once and then performing secondary hot-press forming on the paper pulp molded product.

In one embodiment, the method further includes step S8, recovering the white water, and recycling the white water generated in step S7 to the pulp crushing and diluting step.

Specifically, a steam-water separation barrel 14 connected with the hot-press forming machine 12 and a circulating water barrel 15 connected with the steam-water separation barrel 14 are provided, white water generated by dehydration of the three-section hot-press forming machine 12 in the processing process is injected into the steam-water separation barrel 14 through a pipeline, after steam-water separation, the white water is recovered through the circulating water barrel 15, and the white water obtained from the circulating water barrel 15 is conveyed to the pulper 2 and the pulp distribution barrel 9.

In one embodiment, the steam-water separation tub 14 performs steam-water separation of the white water in the steam-water separation tub 14 by sequentially connecting the vacuum tub 16, the vacuum pump 17, and the vacuum silencer tub 18.

The circulating water tub 15 is also provided therein with a heater and a thermometer for controlling the temperature of the white water to be above 30 ℃.

In one embodiment, a filter is connected between the steam-water separation tank 14 and the circulating water tank 15 to filter impurities (suspended impurities and fine fibers) in the steam-water separated white water.

In one embodiment, the slurry and the white water are transferred to the respective units by a pump 19.

In one embodiment, the pulp molding is prepared by the following steps:

step S1, firstly, the reed pulp board with the mass ratio of 40-45% relative to the total pulp board is injected into the pulper 2 through the batch feeder 1, after 8-9 minutes of mixed pulping, the sugarcane pulp board with the mass ratio of 60-55% relative to the total pulp board is added, and the pulping is continued for 12-13 minutes until the pulping is uniform. The slurry concentration is made to be 5-5.5%. After pulping for 15-17 minutes, the fluorescent whitening agent, the blue dye and the violet dye are added to the pulper 2 in sequence through a reagent barrel 20, with the interval between the addition of each reagent being 90-95 seconds.

The water content of the added sugarcane pulp board and reed pulp board is 8-10%. The whiteness of the sugarcane pulp board is 70-75%. The whiteness of the reed pulp board is 60-65%. The water added into the pulper 2 is deionized water, and the temperature is above 40 ℃.

And step S2, injecting the slurry obtained by the pulper 2 into a slag remover 3, removing impurities, collecting the slurry after slag removal through a first slurry barrel 4, adding the wet strength agent solution into the slurry collected by the first slurry barrel 4 at an interval of 60-65 seconds, and then adding the dry strength agent solution.

Wherein, the volume ratio of the added wet strength agent solution to the total pulp is 1.5-1.7%, and the volume ratio of the dry strength agent solution to the total pulp is 0.5-0.6%.

And step S3, injecting the pulp in the first pulp barrel 4 into the refiner 5 for refining the pulp, and collecting the refined pulp through the second pulp barrel 6, wherein the beating degree of the pulp is controlled to be 27-29 DEG SR, and the pulp concentration is controlled to be 5-5.5%.

In step S4, the pulp in the second pulp barrel 6 is injected into the fluffer 7 for dispersion and fluffing, and the undissociated pulp is injected again into the first pulp barrel 4 through the vibrating screen 8 to be refined again through the refiner 5.

Step S5, the pulp obtained by the fluffer 7 is injected into the pulp mixing barrel 9, water is added into the pulp mixing barrel 9 for dilution, the sizing agent is added into the pulp mixing barrel 9 through the chemical barrel 21 after the pulp in the pulp mixing barrel 9 is diluted for 60-65 seconds until the pulp concentration is 0.2-0.25%, and the diluted pulp is collected through the third pulp barrel 10.

Wherein, the water added in the slurry preparation barrel 9 is deionized water, and the temperature is above 40 ℃.

Wherein the volume ratio of the added sizing agent to the total sizing agent is 1.5-1.8%.

Step S6, the slurry obtained from the third slurry tank 10 is poured into the vortex cleaner 11 to perform vortex cleaning.

And step S7, sucking the slurry obtained by the vortex deslagging device 11 into a three-stage type hot-press forming machine 12, performing primary extrusion forming and secondary hot-press dewatering, and finally performing tertiary hot-press forming to obtain a paper pulp molding product.

Specifically, after 8-9s of pulp absorption, the pulp absorption forming mechanism performs extrusion forming for 25-27s to remove water, the temperature is controlled at 95-100 ℃, the water content of the pulp absorption obtained material is 55-57%, and the pulp absorption forming mechanism performs pulp absorption for 1-2s again to enable the pulp absorption obtained material to reach the required weight; the pulp suction forming mechanism carries out back flushing for 0.5-1s, the air pressure value is 0.7-1.0bar, the air suction vacuum value of the first hot pressing forming mechanism is-0.8 to-1 bar, and the pulp suction obtained object is transferred; the first hot-pressing forming mechanism carries out hot pressing for 20-25s to dewater and form a primary hot-pressing product on the pulp absorption obtained object, the temperature is controlled at 105 ℃ and 110 ℃, and the water content of the primary hot-pressing product is 35-38%; the first hot-pressing forming mechanism carries out back flushing for 0.5-1s, the air pressure value is 0.7-1.0bar, the air suction vacuum value of the second hot-pressing forming mechanism is-0.7 to-0.8 bar, and the first hot-pressing product transfer is carried out; the second hot-pressing forming mechanism carries out hot-pressing forming on the primary hot-pressed product for 43-45 seconds to obtain the pulp molding product, the temperature is controlled at 135-140 ℃, and the water content of the obtained pulp molding product is 2-3%; and the second hot-press forming mechanism performs back blowing for 0.5-1s, the air pressure value is 0.7-1.0bar, and the air suction vacuum value of a receiving mechanism is-0.8 to-1 bar, so that the pulp molded product is transferred to complete hot-press forming.

The pulp molded article produced by the manufacturing method of the above example was on the visual side: 0.2-0.5mm²The number of the salient points is 2, and the salient points are 0.5-0.7mm²And greater than 0.7mm²The bump of (2) is absent, the block sizing of 5mm by 10mm and the linear sizing of 2mm are absent, the linear wrinkles are less than 20mm in total, and the regional wrinkles of 5mm by 10mm are absent. CIE1976L a b color difference was 94.85 for L, 0.62 for a, and-4.74 for b.

The pulp molding manufactured without adding the wet strength agent and the dry strength agent is directly shown: 0.2-0.5mm²The average number of the salient points is 3, and the average number of the salient points is 0.5-0.7mm²And greater than 0.7mm²The total number of the salient points is more than 1 (influencing the appearance), block hanging pulp with the thickness of 5mm by 10mm averagely exists at 1 position, linear hanging pulp with the thickness of 2mm is cumulatively more than 20mm, linear folding is cumulatively more than 35mm (influencing the appearance), and regional folding with the thickness of 5mm by 10mm averagely exists at 1 position (influencing the appearance). CIE1976L a b color difference, L was 94.68, a was 0.58, and b was-4.82.

Pulp moldings made without addition of sizing agent were on a visual scale: 0.2-0.5mm²The average number of the salient points is 5 (more), and the average number of the salient points is 0.5-0.7mm²And greater than 0.7mm²The total number of the salient points is more than 2 (influencing the appearance), block hanging pulp with 5mm by 10mm averagely exists at 1 position, linear hanging pulp with 2mm is cumulatively more than 20mm, linear wrinkles are cumulatively more than 45mm (influencing the appearance), and regional wrinkles with 5mm by 10mm averagely exist at 1 position (influencing the appearance). CIE1976L a b color difference was 94.93 for L, 0.59 for a, and-4.68 for b.

And the pulp molded product manufactured by one-time hot press molding is directly seen: 0.2-0.5mm²The average number of the salient points is 4 (more), and the average number of the salient points is 0.5-0.7mm²And greater than 0.7mm²The total number of bumps was greater than 2 (affecting appearance), 5mm by 10mm of block and 2mm of linear batters were absent, the linear wrinkles accumulated greater than 40mm (affecting appearance), and 5mm by 10mm of regional wrinkles were present on average at 1 (affecting appearance). CIE1976L a b color difference was 94.85 for L, 0.62 for a, and-4.74 for b.

And the pulp molding manufactured by adding no fluorescent whitening agent, blue dye and purple dye is directly printed: 0.2-0.5mm²The number of the salient points is 2, and the salient points are 0.5-0.7mm²And greater than 0.7mm²The bump of (2) is absent, the block sizing of 5mm by 10mm and the linear sizing of 2mm are absent, the linear wrinkles are less than 20mm in total, and the regional wrinkles of 5mm by 10mm are absent. CIE1976L a b color difference was 82.46 for L, -0.32 for a, and 2.47 for b.

The present invention also provides a manufacturing system 100 for manufacturing a pulp molded product. The manufacturing system 100 includes the mechanism mentioned above in the manufacturing method.

According to the manufacturing method and the manufacturing system of the paper pulp molded product, the sugarcane pulp board and the reed pulp board are mixed and pulped in proportion, and the pulping degree and the diluted concentration of the pulp during pulping are controlled, so that the paper pulp molded product formed by hot pressing has smooth surface, less burrs and soft visual sense.

In addition, other modifications within the spirit of the invention may occur to those skilled in the art, and such modifications are, of course, included within the scope of the invention as claimed.