JP6477837B2 - Pulp sheet manufacturing method - Google Patents

Description

  The present invention relates to a method for efficiently producing a low moisture sheet from pulp.

  Pulp produced in a pulp factory is processed into a sheet by a paper machine for production adjustment and external sales, and is temporarily stored as a pulp sheet. Usually, a pulp sheet is made with a paper machine not equipped with a dryer part from the viewpoint of energy saving. Therefore, the obtained pulp sheet has a high water content and is in a state where microorganisms such as fungi are likely to propagate. When the microorganisms propagate, the product value is impaired. Further, when the pulp sheet is sold externally, the pulp sheet is transported by a vehicle such as a truck. However, since the moisture is high, the net pulp content is reduced for the weight. Due to the limitation of the load capacity of the vehicle, a transportation loss is likely to occur, and a large transportation cost is required.

  On the other hand, when the pulp sheet is made with a paper machine equipped with a dryer part, it is necessary to set the rice paper weight low in order to improve the drying efficiency. However, in general, a pulp sheet needs to minimize the paper making chemicals used, such as paper strength agents, in order to increase the purity of the pulp, and the pulp sheet is often not beaten. Can't have paper strength. Therefore, if the rice tsubo is set low in order to improve the drying efficiency, there is a problem of causing operational troubles such as running out of paper at the time of papermaking due to insufficient paper strength. Usually, a pulp sheet is produced by setting a high rice tsubo to prevent operational troubles, and further reducing the paper making speed to supplement the drying efficiency.

  As a method for suppressing the generation of microorganisms such as fungi, a method of applying antiseptic and fungicides using a two-fluid spray in a press part of a paper machine is disclosed (Patent Document 1). If this method is used, the generation of microorganisms such as fungi can be suppressed, but since the moisture of the pulp sheet is high, the problem of transportation loss in the case of external sales is not solved, and further improvement is demanded.

  As a method for efficiently forming a pulp web and reducing the interruption time, an apparatus for controlling the flow rate of dehydrated water using two wire meshes in a wet part is disclosed (Patent Document 2). However, even if this method is used, the load applied to the subsequent dryer part does not change if the rice tsubo is set high in order to prevent operational troubles. It is not possible to improve production efficiency. Thus, a method for efficiently producing a low-moisture pulp sheet that does not cause a problem of transportation loss when selling outside even if the pulp sheet is set high in order to prevent operational trouble has been invented. Absent.

JP 2009-275322 A Japanese translation of PCT publication No. 2002-530547

  An object of the present invention is to efficiently produce a low moisture sheet with little transport loss from pulp.

  The present inventors have found a method for efficiently producing a low-moisture sheet with little transport loss from pulp, and have completed the present invention.

The present invention includes the following inventions.
(1) A method for producing a pulp sheet by passing a pulp raw material containing a lignocellulosic material through a wire part, a press part, and a dryer part in that order to produce a pulp sheet, wherein the pulp part is washed with washing water in the wire part. A method for producing a pulp sheet, comprising washing.
(2) The method for producing a pulp sheet according to (1), wherein the washing water is at least one selected from pure water, natural water, tap water, and industrial water.
(3) The method for producing a pulp sheet according to (1) or (2), wherein the temperature of the washing water is higher than the temperature of the pulp raw material.
(4) The method for producing a pulp sheet according to any one of (1) to (3), wherein a twin wire is used as the wire used in the wire part.
(5) The pulp sheet according to (4), wherein washing water is supplied from a surface opposite to a surface of the twin wire used in the wire part, which is in contact with the pulp material, to wash the pulp sheet. Manufacturing method.
(6) The method for producing a pulp sheet according to any one of (1) to (5), wherein the dryer part is followed by a part that is finished in a flat shape or a wound shape.
(7) The pulp sheet according to any one of (1) to (6), wherein the pulp sheet has a part that continuously performs product packaging after the part to be finished into a flat shape or a winding shape. Production method.
(8) As a product packaging finish, it is characterized by using 1) a device that can continuously wrap a wound product, and / or 2) a device that can continuously wrap a flat product. The method for producing a pulp sheet according to any one of (1) to (7).
(9) Any one of (1) to (8), wherein the winding-shaped product manufacturing apparatus and the flat-shaped product manufacturing apparatus are appropriately selected and switched for use. The method for producing a pulp sheet according to Item.

  According to the present invention, the pulp raw material is passed through the wire part, the press part, and the dryer part in order to produce a pulp sheet by dehydration. In the wire part, the pulp sheet is washed with washing water to improve efficiency. Sheet can be manufactured.

  The pulp raw material containing the lignocellulosic material used in the present invention may be any of dissolving pulp and paper pulp, for example, chemical pulp such as kraft pulp, sulfite pulp, soda pulp, semi-chemical pulp, mechanical pulp, Examples include deinked pulp. These may be used singly or in combination of two or more. In particular, in this invention, it uses suitably for manufacture of the pulp sheet | seat of the dissolving pulp manufactured for the purpose of external sales.

  For the pulp raw material of the present invention, various anionic, nonionic, cationic or amphoteric retention improvers, freeness improvers, paper strength enhancers, internal sizing agents, etc. Internal additives for paper making such as internal additives, dyes, fluorescent brighteners, pH adjusters, antifoaming agents, pitch control agents, slime control agents and the like can be appropriately added within a range not impairing the effects of the present invention.

  The solid content concentration of the prepared pulp raw material is not particularly limited. The solid content concentration is usually adjusted to 0.5 mass% to 5 mass%. When the solid content concentration is 0.5% by mass or less, the load applied to the dehydration process increases, which is not preferable. When the solid content concentration is 5% by mass or more, the fluidity of the pulp raw material deteriorates and adversely affects the pulp sheet formation. It is not preferable.

  The pulp sheet of the present invention is obtained by passing the prepared pulp raw material through a wire part, a press part, and a dryer part in this order to dehydrate them. In the wire part, the pulp sheet is washed with washing water.

  The form of the wire part is not particularly limited, and examples thereof include a long net type, a short net type, a circular net type, and a twin wire type. In the present invention, a twin wire type wire part with good dewatering efficiency is preferable because it leads to efficient production of pulp sheets.

  The supply method of the washing water is not particularly limited, and for example, the washing water can be supplied directly to the pulp sheet or indirectly through a wire using dipping, showering, one-fluid spray, two-fluid spray, or the like. . When a twin wire type wire part is applied, it is preferable to wash the pulp sheet by shower supplying wash water from the surface of the wire on one side opposite to the surface in contact with the pulp raw material.

  The temperature of the washing water is not particularly limited, but is preferably higher than the temperature of the pulp raw material slurry immediately before being supplied to the wire part. The temperature of the washing water is preferably 40 ° C. or higher, more preferably 60 ° C. or higher, and particularly preferably 80 ° C. or higher. By raising the temperature of the washing water, the pulp sheet can be put into the dryer part in a state where the temperature is higher than usual, so that energy required for raising the temperature of the pulp sheet at the beginning of the dryer part can be saved. Efficient pulp sheet production can be realized by converting the saved energy to papermaking speed.

As washing water, natural water such as spring water and well water, pure water such as distilled water, RO water and ion exchange water, tap water, industrial water and the like can be used. As the washing water, at least one of the above can be used, and the washing water can be used in combination or can be used in combination. Although not particularly limited, in the present invention, it is preferable to use pure water as the cleaning water since the cleaning effect of the pulp sheet can be improved. The supply amount of cleaning water is preferably 0.35 to 2.5 L / m ² . By washing with washing water, impurities contained in the pulp can be efficiently removed.

  The press type is not particularly limited, and twin bar press, trinip press, tiger event press, ENP, shoe press, tandem shoe press, baby press, twin wire press, heavy duty press, and the like can be used. One of these or a combination of two or more can be used. Further, the press roll is not particularly limited, and is appropriately selected and combined from rolls provided with rubber covers such as grooved rolls, suction rolls and plain rolls, and resin covers.

  The moisture content of the pulp sheet that has passed through the press part is not particularly limited, but by setting it to 70% by mass or less, the load on the dryer part can be reduced, and an efficient pulp sheet can be produced.

  The dryer type is not particularly limited, and a cylinder dryer, an IR dryer, a hot air type air dryer, or the like can be used, and one of these or a combination of two or more can be used. The moisture content of the pulp sheet that has passed through the dryer part is not particularly limited, but is preferably 20% by mass or less, and more preferably 15% by mass or less in order to reduce transportation loss during transportation for external sales. preferable. The lower limit of the moisture content is not particularly limited, but is preferably 5% by mass or more. If the moisture content is less than 5% by mass, it is necessary to enhance dryer drying, which is not preferable from the viewpoint of energy saving. The passing speed of the pulp sheet is preferably 50 to 150 m / min.

Although the basis weight of the pulp sheet is not particularly limited, but is preferably 400~1200g / ^{m 2,} more preferably ^{600~1000g / m 2, 700~900g / m} 2 is particularly preferred. When the rice tsubo is less than 400 g / m ² , it is not preferable because an operation trouble such as paper breakage may occur in the manufacture of the pulp sheet. When it exceeds 1200 g / m ² , the load of dehydration on the dryer part is high. Since it increases, it is not preferable.

  The pulp sheet that has passed through the dryer part can be continuously finished. The product finishing shape may be a winding shape and / or a flat shape (hereinafter referred to as “part to be finished into a flat shape or a winding shape”). According to the customer's request, it is possible to appropriately select and manufacture a manufacturing apparatus capable of finishing in an arbitrary shape. When manufacturing a rolled-up product, the pulp sheet is once wound on a reel, and the wound pulp sheet is moved to a winder device on the same line as the reel, and is slit and divided to obtain a desired winding. The wound product can be prepared by adjusting the width and length, or the pulp sheet can be directly passed through a winder device without being wound with a reel to prepare a wound product. The rolled-up pulp sheet is subsequently wrapped in an arbitrary wrapping paper and shipped (hereinafter referred to as “part for product packaging finishing”). By continuously performing the wire part, press part, dryer part, flat-finished or wound-up part, and product packaging finishing part, the process up to product packaging can be shortened, thus reducing manufacturing costs. It becomes possible.

  When manufacturing a flat product, the pulp sheet is once wound up with a reel, and the wound pulp sheet is moved to a cutter device on the same line as the reel, and slit and cut to a desired size. It can also be adjusted to a flat product. Further, it is also possible to prepare a flat product by passing the pulp sheet directly through a cutter device without winding it with a reel. The flat-finished pulp sheets are stacked in an arbitrary number, subsequently packed in an arbitrary wrapping paper, and bale-wrapped with a wire before shipment. In addition, the flat-finished pulp sheet can be subjected to a press treatment after stacking an arbitrary number of sheets to reduce the volume and improve the transportation efficiency at the time of shipment transportation.

  In the present invention, from the viewpoint of improving production efficiency, it is preferable that all processes from the dryer part to the product packaging are inline.

<Method for producing dissolving pulp>
Since this invention is applied suitably for manufacture of the pulp sheet which uses the pulp for melt | dissolution as a raw material, although the manufacturing method of the pulp for melt | dissolution is demonstrated below, it is not limited to these description.

The lignocellulosic material that can be used in the present invention may be wood or non-wood, but considering production efficiency, wood with high bulk weight is preferably used. Among woods, broad-leaved wood materials are generally preferred because they have a higher bulk weight than conifers, and some eucalyptus and acacia with a higher bulk weight among hardwoods are preferably used. Applicable broadleaf trees include eucalyptus globulas, eucalyptus grandis, eucalyptus eurograndis, eucalyptus perita, eucalyptus brushana, acacia melanci, etc. It is not particularly limited. Expressed in volume weight value, it is preferably 450~700kg / ^{m 3,} more preferably those of 500~650kg / ^{m 3.} A material having a bulk weight lower than 450 kg / m ³ is disadvantageous from the viewpoint of pulp production efficiency as described above. On the other hand, a material having a bulk weight higher than 700 kg / m ³ is disadvantageous because chemical penetration during pre-hydrolysis or alkali cooking tends to be insufficient, and as a result, pulp quality may be lowered. Hardwood, softwood, and non-wood can be used alone or in combination, and the combination is not limited.

In the present invention, the lignocellulosic material is first heated in the presence of water and subjected to a prehydrolysis treatment. Here, the amount (liquid ratio) of water relative to the lignocellulosic material is 1.0 to 10, preferably 1.5 to 5.0. When the liquid ratio is less than 1.0, water is insufficient, hydrolysis does not proceed sufficiently, and the reaction becomes non-uniform, which is not suitable. If it is higher than 10, the amount of heat required for heating to a desired temperature increases, which is not economical, which is not suitable. The method of adding water is not particularly limited, and water may be added from the outside, the water originally contained in the lignocellulosic material may be used, or when steam is used during heating. May use water contained in steam. In addition to water, chemicals that directly or indirectly assist the hydrolysis of polysaccharides, such as alkalis, acids, and chelating agents, can also be added. The strength of the prehydrolysis of the present invention is 200 to 1000 as a P factor, the temperature is 140 to 200 ° C., preferably 160 to 170 ° C., and the treatment time is determined according to the treatment temperature.
The P factor is the product of the temperature and time at the time of prehydrolysis and is expressed as Equation 1.

  If the P-factor is lower than 200, the acid hydrolysis of hemicellulose is not sufficient, and the subsequent cellulose digestion is not suitable because the cellulose purity of the pulp cannot be sufficiently increased. When the P factor is higher than 1000, acid hydrolysis of cellulose proceeds, and the cellulose purity of the pulp cannot be sufficiently increased. Further, the pulp viscosity is lowered, and the pulp yield is also lowered, which is not suitable. . When the prehydrolysis temperature is lower than 140 ° C., it is necessary to set the reaction time to 10 hours or more, and it is not economical because it is necessary to prepare a huge reaction vessel. On the other hand, when the temperature is higher than 200 ° C., the reaction time may be required to be 0.1 hour or less in some cases, and it becomes difficult to control the reaction, and the material of the apparatus that can withstand such a thermal condition becomes expensive. Therefore, it is not economically suitable.

  The apparatus used in the prehydrolysis step is not particularly limited as long as it can hold the lignocellulosic material in a pressurized state in a water-containing state for a desired time. A digester, a batch kettle, etc. are used. In the prehydrolysis step of the present invention, after completion of the reaction, it is dehydrated or diluted and washed, dehydrated, and sent to the next alkali cooking step. The waste water after pre-hydrolysis is sent to a flash tank, divided into a gas layer and a liquid layer, and flurrals contained in the gas layer are extracted and used to extract hemicellulose degradation products contained in the liquid layer. It is possible to use it.

  Although the apparatus used for the alkali cooking of this invention is not specifically limited, A general purpose continuous cooking kettle, a batch kettle, etc. are used suitably. As the alkali cooking method, known cooking methods such as kraft cooking, polysulfide cooking, soda cooking, alkali sulfite cooking and the like can be used, but considering pulp quality, energy efficiency, etc., kraft cooking method is preferably used. . For example, when kraft cooking wood, the sulfation degree of the kraft cooking solution is preferably 5 to 75%, more preferably 20 to 35%. The effective alkali addition rate is preferably 5 to 30% by mass, more preferably 10 to 25% by mass, based on the mass of the absolutely dry wood. The cooking temperature is 140 to 170 ° C., and the cooking method in which the cooking white liquor is added in portions may be used, and the method is not particularly limited.

  In cooking, as a cooking aid in the cooking solution to be used, known cyclic keto compounds, for example, benzoquinone, naphthoquinone, anthraquinone, anthrone, phenanthroquinone, and nuclear substitutes such as alkyl and amino of the quinone compounds, or the quinone series 1 selected from hydroquinone compounds such as anthrahydroquinone, which is a reduced form of the compound, and a 9,10-diketohydroanthracene compound which is a stable compound obtained as an intermediate of an anthraquinone synthesis method by the Diels-Alder method A seed | species or 2 or more types may be added, and the addition rate is 0.001-1.0 mass% per the absolute dry mass of a wood chip.

  The kappa number after cooking is not particularly limited, but considering the pulp quality and subsequent bleaching properties, for example, when hardwood is used as the raw material, the kappa number is preferably 6-18, and coniferous as the raw material. In some cases, the kappa number is preferably 20 to 35.

  In the present invention, unflooded pulp obtained by a known alkali digestion method is subjected to a bleaching process by a known bleaching method after washing, rough selection and selection steps. Preferably, first, delignification is performed by an oxygen delignification method. As the oxygen delignification method used in the present invention, the medium concentration method or the high concentration method can be applied as it is. However, the medium concentration method in which the pulp concentration is 8 to 15% by mass does not require a special dehydrating apparatus, and the operation is performed. It is preferable because of its good properties. As the alkali used in the oxygen delignification method, caustic soda or oxidized kraft white liquor can be used. As the oxygen gas, oxygen from a cryogenic separation method, oxygen from PSA (Pressure Swing Adsorption), VSA (Vacuum) Oxygen from Swing Adsorption) can be used. The oxygen gas and alkali are added to a medium-concentration pulp slurry in a medium-concentration mixer and mixed sufficiently, and then sent to a reaction tower capable of holding a mixture of pulp, oxygen and alkali for a certain period of time under pressure, and delignified. Is done. The oxygen gas addition rate is 0.5 to 3% by mass per mass of dry pulp, the alkali addition rate is 0.5 to 4% by mass, the reaction temperature is 80 to 120 ° C., the reaction time is 15 to 100 minutes, and the pulp concentration Is 8 to 15% by mass, and other known conditions can be applied. In the present invention, in the oxygen delignification step, it is a preferred embodiment that the oxygen delignification is continuously performed a plurality of times and the delignification proceeds as much as possible. The pulp subjected to oxygen delignification is sent to a washing stage.

  In the present invention, it is preferable to provide a washing stage for each bleaching stage, not limited to the washing stage after oxygen delignification. Examples of the washing machine used in the washing stage include a pressure diffuser, a diffusion washer, a pressure drum washer, a horizontal long washer, and a press washing machine, and are not particularly limited. In each cleaning stage, a single cleaning machine can be used or a plurality of cleaning machines can be used. In the present invention, a cleaning aid such as an alkali, an acid, a chelating agent, and a surfactant can be added to the cleaning water in each cleaning stage. Further, countercurrent cleaning can be performed in which the cleaning wastewater is reused as cleaning water for the preceding cleaning stage.

  In the present invention, the unbleached pulp is preferably sent to a multi-stage bleaching step via an oxygen delignification step. In the multistage bleaching process of the present invention, known ECF bleaching stages such as chlorine dioxide (D), alkali (E), oxygen (O), hydrogen peroxide (P), and ozone (Z) can be used in combination. Later, the aforementioned cleaning stage can be provided. In addition, a high-temperature acid treatment stage (A), an acid washing stage, a high-temperature chlorine dioxide bleaching stage, a chelating agent treatment stage using ethylenediaminetetraacetic acid (EDTA), diethylenetriaminepentaacetic acid (DTPA), etc. are introduced during the multistage bleaching process. You can also. In the multi-stage bleaching process of the present invention, bleaching is performed so that the whiteness of the pulp is 85 to 92% ISO. The whiteness is preferably 87 to 92% ISO, more preferably 89 to 92% ISO. When the whiteness is less than 85% ISO, the whiteness does not reach 90% ISO even if the subsequent peroxide addition treatment is performed under acidic conditions, and the quality as a dissolving pulp is lowered. When the whiteness is higher than 92% ISO, the amount of bleaching chemicals used in the multi-stage bleaching process is excessive and not economical, and in some cases, additional functional groups are introduced into the dissolved pulp, and the dissolved pulp It is not suitable because the quality of

  In the present invention, after the multi-stage bleaching step, the peroxide addition treatment is performed under acidic conditions. The peroxide addition treatment under acidic conditions of the present invention has a pulp concentration of 1 to 40% by mass, preferably 8 to 15% by mass, pH of 1 to 5, preferably 2 to 4, and temperature of 30 to 30. It is carried out at 95 ° C, preferably 50 to 90 ° C. When the pulp concentration is less than 1% by mass, the acid added for adjusting the pH is excessive, which is not economical because it is not economical. When the pulp concentration is higher than 40% by mass, mixing of the pulp and the chemical becomes insufficient. This is not suitable because the reaction becomes uneven. When the pH is lower than 1, the reaction vessel tends to corrode. When the pH is higher than 5, the ash removal effect becomes insufficient, which is not suitable. When the reaction temperature is lower than 30 ° C, the effect of reducing the viscosity of the pulp is insufficient. When the reaction temperature is higher than 95 ° C, a large amount of energy is required for raising the temperature, which is not economical.

In the peroxide addition treatment under acidic conditions of the present invention, an acid can be added in order to obtain an acidic state. The acid may be any of organic acids such as formic acid, succinic acid, and acetic acid, and inorganic acids such as sulfuric acid, hydrochloric acid, and nitric acid, and is not particularly limited. However, relatively inexpensive sulfuric acid, hydrochloric acid, etc. are preferably used. Is done. The peroxide used in the peroxide addition treatment under the acidity of the present invention may be either an organic peracid or an inorganic peracid, and is not particularly limited, but is preferably relatively inexpensive. Hydrogen peroxide, which has no environmental impact even after decomposition, is used. For example, in the case of hydrogen peroxide, the addition rate is 0.01 to 2% by mass, preferably 0.1 to 1.0% by mass, based on the dry weight of pulp.
When the addition rate is less than 0.01% by mass, the effect of addition is hardly observed, and when it is 2% by mass or more, the reaction reaches its peak and the cost increases, which is not preferable. The treatment time is 10 minutes or more, preferably 30 minutes to 180 minutes, but the time is not particularly limited. The pulp viscosity reduction effect due to the addition of peroxide is due to the fact that the cellulose purity of the treatment target is high, so that the reaction frequency of the peroxide and cellulose is high, and the depolymerization is easy. This is considered to be due to the fact that such elements are oxidized, dissolved in water, and easily removed.

  The content of ash contained in the dissolving pulp obtained by the above method is preferably 0.2% by mass or less, more preferably 0.15% by mass or less, and particularly preferably 0.12% by mass or less.

  EXAMPLES Hereinafter, the present invention will be described more specifically with reference to examples and comparative examples, but the present invention is not limited to these examples.

Example 1
<Dissolved Kraft Pulp Paper>
Suspension containing dissolved kraft pulp (hereinafter referred to as “raw material”) is supplied onto the wire from the head box of a twin wire paper machine (manufactured by ANDRITZ), twin wire, twin wire press, heavy duty press, hot air type A pulp sheet was produced by passing through an air dryer in this order. When the suspension containing the dissolved kraft pulp passes through the twin wire, the ion exchange water at a temperature of 85 ° C. is 400 L / min from the surface opposite to the surface in contact with the raw material of the wire on one side (the amount of ion exchange water supplied) : A shower was supplied at a flow rate of 1.4 L / m ² ) to obtain a pulp sheet. The paper making speed at this time was 100 m / min. The absolutely dry basis weight of the obtained pulp sheet was 800 g / m ² . The dryness of the pulp sheet was evaluated according to the following evaluation criteria. Further, the moisture content of the pulp sheet (per dry weight) was measured. The results are shown in Table 1. The obtained pulp sheet was continuously cut into a flat shape and packaged in a bale.

<Evaluation of dryness>
(Evaluation method)
The sensory evaluation of the drying efficiency with a hot air type air dryer was performed as follows.
○: Drying efficiency is excellent and dryer temperature can be set low. ×: Drying efficiency is inferior, and it is necessary to reduce the paper making speed.

(Comparative Example 1)
In Example 1, a pulp sheet was obtained under the same conditions as in Example 1 except that ion-exchanged water was not supplied when passing through the twin wire.

(Comparative Example 2)
A suspension containing dissolved kraft pulp was supplied onto a wire from a head box of a twin wire paper machine (manufactured by ANDRITZ), and passed through a twin wire, a twin wire press, and a heavy duty press in this order to produce a pulp sheet. The paper making speed at this time was 40 m / min. The moisture content of the pulp sheet was measured in the same manner as in Example 1. The results are shown in Table 1. The obtained pulp sheet was continuously cut into a flat shape and packaged in a bale.

  As shown in Table 1, the method of Example 1 yielded a sheet having a low moisture content more efficiently than the methods of Comparative Examples 1 and 2.

  According to the present invention, it is possible to produce a low moisture sheet with high production efficiency and low transport loss from pulp.

Claims (8)

A pulp material containing a lignocellulosic material is passed through a wire part, a press part, and a dryer part in order to dehydrate and produce a pulp sheet,
In the wire part, the pulp sheet is washed with washing water having a temperature higher than that of the pulp raw material .   The method for producing a pulp sheet according to claim 1, wherein the washing water is at least one selected from pure water, natural water, tap water, and industrial water. The method for producing a pulp sheet according to claim 1 or 2 , wherein a twin wire is used as the wire used in the wire part. 4. The pulp according to claim 3 , wherein in the wire part, the pulp sheet is washed by supplying the washing water from the surface of the twin wire opposite to the surface that is in contact with the pulp raw material. Sheet manufacturing method. The method for producing a pulp sheet according to any one of claims 1 to 4 , wherein a part for finishing the pulp sheet into a flat shape or a winding shape is passed after the dryer part. 6. The method for producing a pulp sheet according to claim 5 , wherein a part that performs product packaging is continuously passed after the part that is finished into a flat shape or a wound shape. In the part for finishing the product packaging, 1) an apparatus capable of continuously packaging a rolled product and / or 2) an apparatus capable of continuously packaging a flat-shaped product are used. The method for producing a pulp sheet according to claim 6 . The part for finishing into a flat shape or a winding shape, wherein a manufacturing device for a winding product and a manufacturing device for a flat product are appropriately selected and switched for use. pulp sheet manufacturing method according to 5-7 any one of.