WO1999014424A1

WO1999014424A1 - Pulp production method and apparatus

Info

Publication number: WO1999014424A1
Application number: PCT/GB1998/002712
Authority: WO
Inventors: Vladimir Krotov; James Craig Melville
Original assignee: MELVILLE, Gordon, Brown
Priority date: 1997-09-15
Filing date: 1998-09-14
Publication date: 1999-03-25
Also published as: DE69816478T2; EP1036236A1; ATE245222T1; EP1036236B1; CA2304027A1; DE69816478D1; AU9171298A

Abstract

Apparatus for production of pulp from plant material comprising, in sequence, a first feeder (9) for regulating the input of raw material, a boiler (11) for cooking the material to generate pulp, a second feeder (13) maintained at lower pressure than the boiler (11), a liquid extraction apparatus (15), an unloader (16) in which material is treated with steam, an accumulation reservoir (18) and means for removing pulp from the accumulation reservoir. The first feeder (9) may contain a screw (90, Fig. 4) having a stem (91, Fig. 4) which extends beyond the screw thread, the stem having a passage through which boiler solution is injected. The boiler (11) may contain a substantially vertical screw (111, Fig. 5) having a rotatable, perforated shaft. The liquid extraction (15) apparatus may comprise a screw apparatus containing at least two sets of rotatable cams, each set of cams being of different width. The accumulation reservoir (18) may have a bottom comprising means for keeping the pulp in constant motion.

Description

PULP PRODUCTION METHOD AND APPARATUS

This invention relates to percolation organic solvent boiling of raw

plant materials. Most particularly the invention relates to a unit for cellulose

production from ground hemp stocks from the preliminary hemp processing at

the fibre plants.

From the point of view of pulp production, bast-fibre plants consist of

two different raw materials, the bast which comprises 20-25% of the plant,

and the woody fibres that comprise the remainder of the plant. It was found

initially when using these plants as raw materials that typical pulping

conditions may be optimum for the bast portion but may not be optimum for

the fibrous portion. A more progressive, modern pulping technology of bast

fibre plants such as hemp, flax, and kenaf is based on the separation of stalks

into its two parts: bast (fibre) and woody (shive). The mechanical separation

of stalks by this conventional technology, typically involving stock

preparation and its processing on breaking, scutching and hackling machines,

is not only expensive, but also generates large quantities of waste, including

both dust and chemical waste. A significant proportion of the waste is

irretrievably lost, leading to pollution of the environment. Further, shive

formed during the mechanical separation and cleaning of bast fibres is not

very suitable for pulping by modern methods. In the pulp and paper industry only the bast portion of hemp is used. At present only one technology is known that is capable of eliminating

such wastefulness and converting 60 - 65% of stalks into high quality

bleachable pulp. This technology is based on pulping using aqueous organic

(aqueous alcohol) solutions of ammonia and sulphur dioxide as pulping

liquors. This is known as alcohol-based ammonia-sulphite (AAS) pulping.

AAS pulping is unrivalled in both the selectivity and the extent of

delignification of the raw plant materials.

In the International Review for the Pulp and Paper Industry, Sterling

Publishing Pic, 1994, pp. 67 - 70, V. Krotov discusses a method of using AAS

technology involving drip percolation. The principle involves the trickling

and drip percolation of pulping liquor (consisting of alcohol based ammonia-

sulphite) through the layer of lignocellulosic material (chopped hemp, straw,

shive, etc) in vapour / gas medium. The pulping was carried out at low liquor

ratio close to that of vapour phase digestion. The liquor is continuously

recovered by condensation before trickling.

A unit incoφorating this technology was reported by Krotov V. S.

and Lavrinenko T. F. in the 4th International Symposium of Scientists from

Comecon Countries, Theses, Zinatne, Riga, 1982. This was a closed cycle

system unit which contained the following components sequentially: a tank

for chemical mixing, a first scrubber to which an exhauster is connected, a

second mixing tank for ammonia water, a condenser, a second scrubber, third

and fourth tanks, a hopper, a feeder, a spiral conveyor, a digester, a discharge unit, a fluffer, a discharge tank, an evaporator, a flasher, a moisture trap and a

cyclone.

The most immediate advantage of this single unit plant was that it

could integrate all major processes of pulp production including raw material

impregnation and cooking, stock washing and dewatering, recovery of the

liquid fraction of a spent solution, collection and utilisation of dirty

condensates, utilisation of secondary steam and condensate heat, and

collection and removal of non-condensable gases without air entrapment.

One factor that contributes to the efficiency of this pulping method

within this unit is the retention of initial shape of the raw material particles

during the whole process of AAS delignification. The delignified stock is turned into pulp under very limited mechanical action.

A significant advantage of this drip percolation and the unit disclosed

by Krotov et al. was the effective reduction in environmental pollution. It is

ensured by the closed-cycle production which is carried out in a space entirely

isolated from the environment, with complete absence of effluents, including

dirty condensates. Non-condensable gases are collected without entrained air

and can be taken for neutralisation. This differs from multi-unit plants with a

great number of unpressurized vessels where gas emissions are distributed

along the production line, entrain air and are inevitably released into the atmosphere. Before the raw material enters the digester, it undergoes a process

known as Prex impregnation. A small portion of the raw material within the

feeder apparatus (for a digester) is compressed and then expanded. At the

point of expansion, the pulping liquor is injected into the feeder apparatus,

whereby the raw material acts as a sponge and absorbs the liquid. This

technique allows a significant proportion of the raw material to come into

contact with the pulping liquor. However, it is unlikely that using the

disclosed apparatus results in all the material being saturated. There thus

exists the possibility of improving the technique by developing an improved

feeder apparatus. Further, the prior art document does not discuss variations in

condition, such as temperature for example that might improve this method of

impregnation.

In this prior art unit the only cooking of the raw material occurs within

the digester. It is possible that the efficiency of delignification could be

improved by allowing^" some preliminary cooking prior to the material entering

a digester or equivalent apparatus. There is also the problem with the design

of the digester disclosed that the means by which the cooked and washed pulp

is removed from the digester into the discharge unit is inefficient and this can

lead to a congestion of material. There is scope for improvement of the means

by which the material is removed from within any cooking device used.

Within this unit there is significant recovery of the components of the

spent pulping solution / liquor. For example, up to 60-70% ammonia and up to 50% sulphur dioxide can be recovered quantitatively. Organic solvent can

also be recovered quantitatively. However, there still exists the possibility of

improving the recovery of the liquid fraction of the spent solution.

The present invention seeks to create an improved single, closed unit

which can be operated continuously for cellulose production from fibrous raw

plant material. The unit in an embodiment must use AAS pulping technology

and drip percolation and thus retains the advantages of these methods of

delignification. As with the previously disclosed pulping unit using this

technology, the unit must simultaneously perform the operations of saturation

of the raw plant material by boiler solution, boiling (delignification) of the

raw plant material, washing of the fibrous product, regeneration of the organic

solvent, residue water and chemicals from the used boiler - washing solution,

dehumidification of the washed fibrous product, collection and absorption of

the steam and gases and preparation of the boiler solution from the recovered

and fresh chemicals. ^'However, most importantly, the unit according to this

invention seeks to provide for improved Prex impregnation of the raw

material.

A further object of the invention is to improve the processing of the

washed and cooked plant material and in particular to improve the efficiency

of the collection - particularly from the cooking apparatus - dewatering and

predrying of the fibrous product (pulp). Also the invention seeks to improve

the collection, condensation and absorption of vapours released in the delignification, the collection, cleaning and centralised discharge for

neutralisation and utilisation of non-condensable gases and also the

preparation of pulping liquor from the recovered chemicals.

Another object of the invention is to produce a unit which realises few

waste products, and does not need fresh water technology or gas treatment

facilities for processing the raw plant material into high quality cellulose. The

unit should be raw material, cost and energy efficient.

According to the present invention there is provided an apparatus for

the production of pulp from raw material by drip percolation comprising in

sequence a first feeder for regulating the input of raw material into a boiler,

containing a screw having a prolonged stem which extends beyond the screw

thread, the stem having a passage through which boiler solution is injected

into the first feeder, a boiler for cooking the raw material to generate pulp, a

second feeder which receives cooked material from the boiler and which is

maintained at a lower pressure than the boiler, a liquid extraction apparatus

for extracting liquid from the cooked material passed into it; an unloader

which is maintained at a lower pressure than the liquid extraction apparatus, in

which material received from the liquid extraction apparatus is treated with

steam, an accumulation reservoir for receiving pulp from the unloader and a

means for removing pulp from the accumulation reservoir.

Preferably the unit is composed of two sections whereby the first

section for the preparation of the boiler solution comprises: a first mixing device into which water is fed, a plunger pump with adjustable inputs, a first

scrubber into which ammonia is fed by a first output tank, a first 'tube in

tube' heat exchanger, a second scrubber the contents of which are fed into a

second tank; and the section for the boiling of the raw material comprises; an

input bunker, a spiral feeder, an inclined spiral conveyor, a boiler, a second

mixing device, a second 'tube in tube' heat exchanger, a rotor feeder, a

dividing bunker, a screw apparatus, a screw unloader, a fluffer, an

accumulation reservoir, a screw conveyor, a first casing tube heat exchanger, a

fourth output tank, a first vaporising apparatus, a steamer, a second casing

tube heat exchanger, a fifth output tank, a second vaporiser apparatus, a third

vaporiser apparatus, a first cyclone, a third casing tube heat exchanger, a

second cyclone, an emergency tank, a helper bunker, a fourth casing tube heat

exchanger, and a system of pumps and interconnecting tubes.

The construction of the unit is described by reference to the appended

drawings in which:

Figure 1 is a schematic of the boiler solution preparation section of the

unit; Figure 2 is a schematic of the section of the unit for boiling the raw

plant material;

Figure 3 is a cross-section along the line A - A' through the input

bunker for the raw material;

Figure 4 is a cross section taken along the line B - B' through the

spiral feeder of the unit;

Figure 5 is a cross-section taken along line C - C through the boiler

of Figure 2;

Figure 6 is a cross-section taken along the line D - D' of the screw

apparatus;

Figure 7 is a 'section taken along line E - E' of the accumulation

reservoir of Figure 2; and

Figure 8 is a section taken along the line F - F' of Figure 7.

The two sections that together comprise the unit are respectively

shown in Figures 1 and 2. The two sections are not separate entities but are

constructed to interlink through specific pieces of apparatus; the two sections

together form the closed cycle of the unit. Figure 1 relates to the section for the preparation of the boiler solution.

or this, ammonia water with an ammonia concentration between 25 and 27%

is used, as well as sulphur dioxide, technical (95%) ethanol and water. Water

for the preparation of the boiler solution is supplied into the mixing device 2,

which can also serve as a pot for the preparation of hard or liquid chemicals.

The water is sent via the means of the plunger pump with adjustable input 7,

7a (working and spare respectively) from the mixing device 2 to the first

scrubber 3 which is in the tail. Condenser 28 supplies non-condensable gases

in to the first scrubber 3 where they are absorbed by the water which thus

removes impurities. Non-purified gases also enter the first scrubber from the

second scrubber 4.

The section for the preparation of the boiler solution is hermetic and

works under raised pressure. The first scrubber 3 works under atmospheric

pressure, and in the all the following apparatuses the pressure is slowly raised depending on the aerohydrodynamic resistance.

The weak solution from the first scrubber 3 goes via the pump 7b

through the first 'tube in tube' heat exchanger 5 to the second scrubber 4. The

'tube in tube' heat exchanger has a different temperature within the tubes than

between the tubes. The temperature within the tubes is considerably lower

than that between them, typically the inside of the tubes being between 25 and

75 degrees Celsius and that between the tubes being about 100 degrees. When gases are absorbed in the scrubbers, heat may be emitted and the

solution is warmed up to 45 - 50°C. The heat exchanger 5 ensures that the

temperature of the solution is no more than 20°.

Sulphur dioxide is fed into the second scrubber 4 from the tank

system. Sulphur dioxide feeding is also provided for the scrubber 3 as well.

The scrubber 4 is also supplied with ammonia water for irrigation from the

output tank 6 by the pump 7c. The output tank 6 is equipped with injectors,

from which water is supplied to ensure safety of the servicing.

The solution from the second scrubber 4 is fed by the pump 7d to the

tank with ready boiler solution, the mixing device 2a.

Plunger pumps with regulated flow 7a, 7b, 7c and 7d work without

reserve but the scheme allows for these pumps to be interchanged.

Figure 2 shows the section of the unit for the boiling down of the raw

plant material, typically composed of ground down hemp stock from the

fibre plants. The raw 'material comes from storage into the input bunker 8.

Unlike the hopper used in the prior art units, the input bunker 8 is situated

immediately above the loading carbine of the spiral feeder 9 as illustrated in

Figure 2.

The input bunker 8 itself is illustrated in Figure 3. It is equipped with a

stirring device 80 which prevents raw material from getting stuck, as well as

with a screw 81 for pressing the raw material. The stirring device 80 is

typically rotated at between 0.25 and 0.52Hz (15 and 31 rotations per minute). The number of arms of the stirring device 81 is not limited to the two

illustrated in the figure, but can be varied according to the required input rate

of the raw material. The amount of raw material passing through the input

bunker 8, and also the extent to which the raw material is pressed are

controlled by changing the spinning speed of the screw 81, the speed being

controlled by a thyristor converter. Such a converter serves as a control over

the engines driving the equipment.

Preferably, the input bunker 8 according to this invention will have a

working volume of not more than 1.8 cubic metre. This volume ensures that

the raw material is efficiently pressed before passing out of the bunker 8.

Input and output from the bunker 8 are closely controlled such that the

productivity of bunker 8 is within the range of 3.7 to 10.0 cubic metres / hour.

The pressed raw plant material is loaded from the input bunker 8

directly into the spiral feeder 9 situated immediately beneath it. A cross-

section through the ^"feeder 9 (along the line illustrated in Figure 2) is

illustrated in Figure 4. The purpose of the feeder 9 is to further regulate the

movement of the raw material to ensure a continuous flow of raw material

into the boiler 11. The feeder 9 consists of cylindrical and conical parts, as

well as a screw 90 which extends the entire length of the feeder 9. The shape

of the screw by analogy to the shape of the feeder itself, has both cylindrical

90a and conical 90b parts. The diameter of the screw decreases as it passes

from the cylindrical to the conical part of the feeder 9, as illustrated in figure 2. Unlike prior art feeders 9, the screw of this feeder has a prolonged stem 91

which extends beyond the screw thread in the conical region 90b of the screw

90.

In the conical part of the feeder 9 the raw material is compressed, and

because of the slow decrease in the diameter of the screw, a plug is formed

which resists the pressure of the boiler 11 - the relative positions of the boiler

11 and the spiral feeder 9 being illustrated in Figure 2 - and ensures the boiler

11 is airtight. The purpose of the prolonged stem 91 of the screw is to create a

hole in the centre of the compressed plug. When the plug comes off the end

part of the screw 90, the raw material is depressurised. In the zone where this

depressurization occurs there is a hollow shaft 92 through which boiler

solution is injected. With the help of needle valves situated around the

perimeter of the output opening of the spiral feeder 9, the boiler solution

irrigates the outside surface of the raw material plug. Also as the raw material

is depressurized it, similarly to a sponge, absorbs the injected boiler solution

such that a fast saturation of the raw material occurs. When the load drops to

70% the feeder engine is shut off and the output opening of the feeder is

closed off by closing the disc of a hydrocylinder.

The boiler solution is fed through the hollow shaft 92 in the spiral

feeder 9 by the pump 7f, 7g (working and spare respectively) from the

apparatus 2a. The solution from 2a passes through the heat exchanger 5a, where it is heated to temperature of 75°C. As with the input bunker 8, the spinning speed of the spiral feeder's

screw 90 determines the efficiency of compression of the raw material. The

speed of rotation also determines the time for which the raw material remains

in the feeder 9; typically the throughput of the feeder 9 is maintained at a

similar level to that of the input bunker 8. However, unlike the input bunker 8

which is at room temperature, the spiral feeder 9 is maintained at a

temperature of approximately 100°C. This preliminary temperature increase

of the raw material enables some preliminary cooking of the material when it

is first impregnated with boiler solution in the depressurization zone of the

feeder 9. Obviously most cooking occurs in the boiler 11 later in the unit, but

the temperature increase in combination with this initial impregnation ensures increased cooking efficiency within the unit as a whole. The impregnation of

the material is further improved by the hole in the centre of the plug generated

by the prolonged stem of the screw 91.

The feeder contains attachments such that different screws 90 can be

mounted within it. Obviously these screws will have both cylindrical 90a and

conical 90b parts in correspondence to the shape of the feeder 9 but can differ

in the length and diameter of the prolonged stem 91. This allows for the

possibility of varying the size of the hole formed in the plug as it is extruded

from the conical end 90b of the screw. As discussed, the hole is important

for the impregnation of the central part of the raw material plug. However, no

batch of raw material will be identical and changing the prolonged stem will allow for more efficient impregnation of material that may vary in fibrous or

bast composition. It is also useful where the unit is adapted for use in

processing different types of bast-fibred plants.

With the help of the inclined spiral conveyor 10, the raw material is

sent to the lower part of the boiler 11, which is equipped with a vertical screw

111 that moves the raw material up and down and rods that both loosen the

pulp and preclude the appearance of dense and stagnant zones in the boiler 11.

In the lower part of the boiler 11 the raw material is submerged in

boiler solution. This is pumped from the second mixing device 2a by pump 7f

into the boiler through the vertical screw 111 which has a perforated shaft.

The level of the liquid is regulated by controlling the flow of the solution

entering the boiler 11 and also by pumping away the used solution, through

two circular pockets (not shown), protected by two to three rows of circular

sieves (not shown), using the pumps 7h and 7i. The pockets together with the

sieves are vital for changing the liquid level; this control is essential as it

allows for the efficiency of the delignification process to be maintained even

if slight fluctuations in raw material volume entering the boiler 11 occur. Any

solution pumped out through the pockets in this way is heated in the casing

tube heat exchanger 19 and returned to the boiler 11 through the perforated

shaft of the vertical screw 111.

Importantly, the temperature and pressure conditions of the boiler 11 are strictly controlled The temperature is maintained at 170±10°C throughout the circulation of the boiler solution. The working pressure of the boiler is

held at not more than 1.3MPa. The boiler 11 is equipped with a preventive

valve, which will open at the pressure of 1.5MPa and also with features which

allow for unloading of the boiler 11 when the pressure is raised. Unloading

the material from the preventive valve is done into the tank 6b with the casing

tube heat exchanger 22a. Those gases that do not condense in heat exchanger

22a, pass through cyclone 32 into the heat exchanger 28.

Raw material in the boiler 11 is raised from the liquid and enters into

a steam and gas zone, where it is subjected to boiling and irrigation with drops

of liquid condensed from the steam of the used solution on the surface of heat

exchanger-condenser 25. Consequently, there is simultaneous washing and

boiling of the fibrous product. The boiler-washing liquid used for irrigation

becomes saturated with the reaction products. As the raw material rises further

from the level of liquid it can be additionally heated by steam, supplied

through a carbine in the middle part of the boiler 11.

In the upper part of the boiler 11 a coil of the reverse screw 116 with

spirally welded ribs 117 is provided. The reverse screw 116, besides

preventing the pulp from entering the steam portion of the boiler 11, also

serves to distribute the irrigation liquid. As boiling liquid enters the boiler 11

it strikes the reverse screw 116 and the ribs serve to break up the stream and

thus disperse the liquid over a larger area. This ensures that as large a portion of the raw material as possible comes into contact with the irrigation liquid

and improves the effectiveness of the drip percolation.

It is also possible to change the spinning speed of the boiler shaft 112

using a thyistor converter. Typically, the shaft is rotated at about 0.53 Hz (32

rotations/min.).

The rate at which the pulp is raised through the boiler 11 is controlled

such that it spends between 1 and 4 hours within the boiler 11. This ensures

sufficient boiling and washing of the raw material. Additionally any gases

released from the upper part of the boiler are blown away through tank 6b.

In the prior art unit shown in the 4th International Symposium of

Scientists from Comecon Countries, Theses, Zinatne, Riga, 1982, the pulp passes from the boiler into a stepped series of screw feeders referred to as the

discharge unit. The pulp is subjected to limited compression within this

apparatus, which serves to press out some of the pulping liquor remaining in

the material. In the present invention the raw material passes through a

sequence of apparatus components which greatly improves the ease of

removal of the material from the boiler 11 and which result in far more

effective removal of liquid from the washed and boiled pulp.

Firstly, the resultant boiled and washed pulp is unloaded from the

upper part of the boiler by the spiral conveyor 12. The pulp is supplied to the

conveyor 12 by means of paddles 118 which are illustrated in Figure 5. The paddles are mounted on the rotating boiler shaft and thus the unloading

process is regulated by varying the speed of rotation.

One important feature of the spiral conveyor is its high speed of

rotation. The screw within it is rotated at approximately 16.7 Hz (1000 rot /

min). This ensures a very high rate of throughput and helps to prevent

congestion of the pulp at the top of the boiler.

Pulp unloaded in this way passes from the spiral conveyor 12 into a

rotor feeder 13. The pressure in the rotor feeder 13 is lower than that of the

boiler (1.3MPa), and is typically maintained at c. 0.7MPa to ensure an

approximate pressure difference of 0.6MPa. Secondary boiling gases from the

boiler 11 expand on entering the rotor feeder 13 allowing for their separation and removal.

The rotor feeder 13 supplies the pulp into a dividing bunker 14. This is

constructed in the same way as the input bunker 8 and thus consists of both

conical and cylindrical parts, and also comprises a corresponding stirrer 14a

(within the conical part) and a pressing screw 14b (within the cylindrical

region). The action of the stirrer 14b prevents the raw material getting stuck as

in the input bunker 8. Again the screw 14b serves to compress the pulp and

consequently squeeze liquid from the material.

The use of a dividing bunker 14 gives far more efficient pulp

compression. The spinning speed of the pressing screw 14b can be varied which allows for greater control of both the throughput of pulp and the extent

to which the pulp is actually compressed.

From the dividing bunker the cellulose pulp is loaded into the screw

apparatus 15, where extra liquid is pressed out. This apparatus is illustrated in

Figure 6. The loading sequence is maintained airtight by fitting the screw

apparatus 15 with a closing device. In emergency situations the rotors of the

closing device are set to a closed position, by which a steep decline of

pressure of the system is prevented.

After closing the device the cellulose pulp is ground in the block of

cams. These blocks are shown in detail in Figure 6. Along the length of the

screw apparatus 15 the cams is varied; in Figure 6 there are three identified

types of cam (150, 151, 152) which are interchanged as illustrated. This arrangement of cams is in no way limiting. Other cams can be used, or the

order of the cams changed. The variation of cams within the screw apparatus

15 means that the pulp is ground with variable intensity along its length,

which improves the efficiency with which extra liquid within the pulp is

squeezed out. The rotation of the screw is typically maintained between 1.6

and 3Hz (100 to 180 rotations / min). It is also possible for each different type

of cam to be rotated at a different frequency by connection of each part to a

different driving engine.

Having passed through the screw apparatus 15 the pressed pulp is

unloaded into the screw unloader 16 which serves to both unload and steam the cellulose pulp. Typically the screw unloader 16 is maintained at a pressure

between 0.1 and 0.2 MPa such that gases are removed by the lowering of

pressure. Additionally the screw unloader 16 is supplied with steam to take

away the remnants of alcohol. The temperature of the pulp entering the screw

unloader 16 is approximately 150°C but within this apparatus the temperature

is set at lOO°C.

From the screw unloader, the pulp is transported to the fluffer 17,

which is designed to divide larger pieces of the pulp into separate packs of

fibre so as to facilitate the process of blowing away and removal of the highly

volatile fraction of any liquid still contained in the pulp. The fluffed up pulp

then is sent to the conical accumulation reservoir 18 shown in Figure 7. In the

upper part of this reservoir 18 there is an aperture through which steam is

blown for the purpose of removing alcohol and other volatile species from

the pulp. To prevent significant condensation of this steam, the reservoir 18 is

maintained at a temperature of approximately 100°C.

Unlike the discharge tank shown in the unit in the 4th International

Symposium of Scientists from Comecon Countries, Theses, Zinatne, Riga,

1982, this accumulation reservoir 18 has a 'live bottom' formed by four

screws, as illustrated in the cross-section of Figure 8. Preferably the four

screws have identical diameters and are divided into two sets 181, 182 each

set rotating out of step with the other. The screws are driven by a motor such that they rotate at a speed of between 15 and 30 rotations per minute. This

serves to keep the pulp in constant motion.

The choice of identical screws is only one possibility. Conceivably,

the diameter of each screw or set of two screws could be different, or each

screw could be attached to a different motor such that they rotate at different

speeds if this improves the efficiency with which the steam blown into the

apparatus removes alcohol or other remaining volatile liquids still remaining

in the pulp after fluffing.

The cellulose pulp passes out of the accumulation reservoir on to a

screw conveyor 18a for packing. The screw acts upon the pulp to press out

any further liquid (filtrate) from it; liquid collected in this way is gathered in

the apparatus 6c, which also receives the condensate from the heat exchanger

(condenser) 22. The apparatus 6c is maintained at the same pressure as the

screw apparatus 15, c. 0.7MPa. From apparatus 6c the boiler solution is

recycled by pump 7j to the boiler 11 for use in irrigation of the raw material.

The extra solution flows from the apparatus 6c to vaporising apparatus 20,

where the pressure is lowered. When necessary the extra solution is sent by

the pump 7k out of the system.

Used boiler solution is concentrated in a steamer apparatus 24

equipped with a flowing down pellicle consisting of a series of parallel tubes

25 as illustrated in Figure 2. This steamer apparatus 24 is made with a

separate heating tank and a separator 26. The temperature within the tubes is maintained about 15°C lower than the temperature in between the tubes.

Preferably, the temperature in the tubes is set at 175±5°C whilst that in

between the tubes is set at 190±5°C. In line with the main theme of the unit

the pressure inside the steamer apparatus is also closely controlled. Preferably

the working pressure inside the tubes is set at 1.25±0.05MPa and that between

the tubes is also set at 1.25±0.05MPa. For effective boiling down of the used

boiler solution the steamer must have a large surface area; the working

surface area of a typical steamer according to this invention is about 25m .

From the boiler the solution enters the separator 26 from where it is

pumped by pumps 7n and 7o (working and spare respectively) into the upper

part of the steamer apparatus 24; the solution comes through a distribution

device in the steamer apparatus 24 and flows down evenly on the inner

surface of the tubes 25 in the form of a thin layer. Simultaneously the

solution is being boiled down to the required concentration. The gases

released in the steamer pass into the heat exchanger 27 (condenser). The

condensed boiler solution is collected is gathered in tank 6d and later sent by

pump 7m to the boiler 11 for irrigation. The extra solution from the tank 6d

flows into the vaporiser apparatus 20a - which is maintained at a lower

pressure - and if necessary is pumped away to be used in preparation of the boiler solution. The concentrated boiler solution from the steamer apparatus is sent

away to the vaporiser apparatus 20b, where it is further boiled down and

collected in the an output tank.

The gases separated in the vaporiser 20b are sent through a first

cyclone 31 to the 'casing-tube' heat exchanger 28. Secondary gases from the

screw unloader 16, from the vaporisers 20 and 20a are also sent to this heat

exchanger 28 through the second cyclone 32. The purpose of both cyclones

31, 32 is to catch fibres supported within the gases of the boiler solution. Both

cyclones are held at a temperature of 100°C and work at atmospheric pressure.

The first cyclone 31 has however a smaller working volume than the second cyclone 32 which directly relates to the relative volumes of gas circulated to

each of them.

The condensed liquid is sent to the tank 2a and non-condensable gases

go to scrubber 3 for the absorption and cleaning process. The pulp caught in

the second cyclone 32-is periodically unloaded from it into a helper tank.

In the unit a means of emptying the contents of the boiler 11 in

emergency is provided. There is an emergency tank 30, equipped with a stirrer

and a net for removing drops of liquid. The lower part of the boiler 11 is

connected through a blower tube 34 to the middle part of the emergency tank

30. When the pressure is lowered - the tank's working pressure is typically

atmospheric pressure - secondary boiling gases form in the emergency tank

30, which pass through the second cyclone 32 into the condenser 28 and later into the first scrubber 3. The incoming solution from the boiler has a

temperature of approximately 170°C but this is lowered to 100°C within the

tank 30. At this point it is needed to maximise the usage of cooling water for

the condenser 28 and the irrigation liquid Cl. The emergency tank 30 is

unloaded periodically into the movable helper bunker 35.

Compared to the prior art unit of Krotov the unit of the embodiment of

the present invention comprises two more vaporisers throughout (described as

flashers in the prior art document). The function of each vaporiser apparatus

is to lower the pressure and temperature of the boiler solution passing through

it. The three vaporisers are of identical volume and all work at atmospheric

pressure. Their increased number and their respective positions within the unit

serve to improve the temperature efficiency of the apparatus. This contributes

to an improvement in the preparation of the pulping liquor from recovered

chemicals in this embodiment compared to the prior art unit.

Before a planned stop of the unit, the boiler solution must be taken

away from the boiler. For this purpose,- pump H7 directs the boiler solution

into a diversionary path not encountering the heat exchanger T.

A number of the apparatus components are of standard construction

within the field of pulping. The standard equipment include the mixing

devices 2, 2a which are fixed with turbine mixers, the tanks (6 to 6e) and all

pumps. With respect to the standard pumps used, these have a maximum

working pressure flow of 16 kg/cm². The automation scheme of the unit provides for blocking of the pumps when the pressure inside exceeds this

value.

The basic construction material for the unit is steel and more

particularly most component apparatus are constructed from carbon steel.

However, it is possible that the unit could be constructed from other materials

with similar mechanical and chemical properties as steel, for example the

resistance to the pH conditions within the boiler. The carbon steel may also be

treated to enhance its resistance to corrosion or subjecting it to other

preservation processes.

The unit of the embodiment does contain more component parts than

the aforementioned prior art pulper. The importance of the increased number

of vaporisers has already been discussed. Despite this increase the unit can be

constructed in compact form such that it requires little more floor space than

the known unit. The embodiment can be constructed as a highly-profitable

low-capacity plant which even offers scope for the development of mobile

units that can be used in the growing regions for the raw materials. The

integration of the individual parts and assembly units of the invention is

indicated by its high level of unification. The invention has a typical

coefficient of unification of 52%.

The unit, although particularly suitable for ground hemp stocks, is not

restricted to this type of raw material. Other bast-fibred plants such as flax or

kenaf are obvious alternatives. These would require a different composition of pulping liquor i.e. a different relative proportion of components and also a

different cooking and treatment time. The throughput of material through the

unit can readily be varied to allow for this.

Example:

The following example illustrates the typical construction and

operation details for a unit according to this invention. The unit described

hereafter may be used for the production of cellulose at a rate of no more than

300 kg/hr. The conditions listed are the optimum for this total productivity

limit.

Table 1

to

C σ v>

H

H C H m

0) x m m

H

3)

C r- m

M σ>

Other technical characteristics are:

Maximum working pressure of the steam supplied for heating, Mpa;

- to the boiler (11) 1.6

- to the steamer (24) and the heat exchanger (19) 1.3

- to the screw unloading device (12) 0.05

- to the second 'tube in tube' heat exchanger (5a) 0.05

Working temperature

- of the cooling water 25°C

- of the cooled water 7 - 18°C

Time pulp spends in the boiler 1 - 4 hrs

pH of the environment 4.5 to 13

Density of raw material in the input bunker 80 - 125 kg/m

Specific energy consumption,

kWt/ton, kg/hr, not more than 676

Maximum steam usage, kg hr

- with pressure of 1.6 MPa 40

- with pressure of 1.3 MPa 481

- with pressure of 0.05 MPa 84

The volumes and operating temperatures and pressures represent the

preferred values but are not limiting. The size of each component of the unit

can be varied according to its location. For example, if a mobile unit is

required, the dimensions of each piece of apparatus comprising the unit will be reduced correspondingly in scale. The unit is of direct importance to

countries where wood supplies are limited and the unit must be sized

according to the regional growth of bast-fibred plants and the associated

demand of paper.

The amount of ethanol used is not given. This raw material is only

supplied for the start-up of the unit since during pulping methanol, ethanol

and acetone as formed from the components of the fibrous raw material, this

being a well-known effect of the AAS delignification method. Subsequently,

as organic components are accumulated in the pulping liquor, ethanol can be

recycled. Excess organic solvent can be drawn and processed as a market

chemical. Hence in a continuously operating unit there is no need to supply

ethanol.

Claims

1. An apparatus for the production of pulp from raw plant material comprising in sequence; a first feeder for regulating the input of raw material into a boiler, containing a screw having a prolonged stem which extends beyond the screw thread, the stem having a passage through which boiler solution is injected into the first feeder; said boiler for cooking the raw material to generate pulp; a second feeder which receives cooked material from the boiler and which is maintained at a lower pressure than the boiler; a liquid extraction apparatus for extracting liquid from the cooked material passed into it; an unloader which is maintained at a lower pressure than the liquid extraction apparatus, in which material received from the liquid extraction apparatus is treated with steam; an accumulation reservoir for receiving pulp from the unloader; and means for removing pulp from the accumulation reservoir.

2. An apparatus according to claim 1 whereby the first feeder consists of both cylindrical and conical ..parts, the prolonged .stem of the screw extending beyond the conical part of the screw thread.

3. An apparatus according to claim 1 or claim 2 wherein the prolonged stem is of variable length and diameter.

4. An apparatus according to claim 1 wherein the boiler for cooking the raw material to generate pulp contains ^"a substantially vertical screw having a rotatable, perforated shaft.

5. An apparatus according to claim 4 wherein the boiler further comprises a reverse screw of opposite sense to the substantially vertical screw.

6. An apparatus according to claim 5 wherein the reverse screw has at least one spirally extending rib.

7. An apparatus according to any of claims 4 to 6 wherein the boiler further comprises paddles for removing cooked material from the boiler, said paddles being mounted on the shaft of the substantially vertical screw.

8. An apparatus according to claims 1 to 7 wherein the liquid extraction apparatus for extracting liquid from the cooked material comprises a screw apparatus containing at least two different rotatable cams.

9. An apparatus according to claim 8 whereby each cam within the screw apparatus is arranged to be rotated at a different frequency.

10. An apparatus according to any of claims 1 to 9 wherein the accumulation reservoir has a bottom which comprises means for keeping the pulp in constant motion.

11. An apparatus according to claim 10 wherein the bottom of the accumulation reservoir is formed by rotatable screws.

12. An apparatus according to claim 11 wherein at least one of said screws in the accumulation reservoir rotates out of step with the other screws.

13. An apparatus according to claim 12 wherein two of said screws in the accumulation reservoir rotate at the same frequency.

14. An apparatus according to any of claims 11 to 13 wherein each of said screws in the accumulation reservoir may be of different diameter.

15. A apparatus according to any of claims 1 to 14 further comprising a first bunker, positioned on top of the first feeder and which supplies raw material into the first feeder, said first bunker including a stirring device and rotatable screw.

16. An apparatus according to any of claims 1 to 15 further comprising a conveyor, positioned between the boiler and the second feeder, which receives cooked material removed from the boiler.

17. An apparatus according to any of claims 1 to 16 further comprising a second bunker for compression of the cooked material, positioned between the second feeder and the liquid extraction apparatus, said second bunker comprising a stirrer and a pressing screw.

18. An apparatus according to any of claims 1 to 17 further comprising a fluffer, positioned between the unloader and the accumulation reservoir, which divides the cooked material into separate packs of fibre to facilitate liquid removal from the material.

19. An apparatus according to any of claims 1 to 18 wherein the means by which pulp is removed from the accumulation reservoir comprises a screw conveyor.

20. An apparatus according to any of claims 1 to 19 further including means for producing boiler solution and supplying this boiler solution to the boiler and / or first feeder, said means comprising; a mixing device into which water is supplied; a first scrubber which receives water from the mixing device and into which sulphur gas is supplied to generate a weak solution; a heat - exchanger through which the weak solution from the first scrubber passes; a second scrubber which receives the weak solution from the heat exchanger and which is supplied with ammonia water and sulphur dioxide gas; an output tank into which the solution from the second scrubber is passed and in which the boiler solution is generated; means for transferring the boiler solution from the output tank to the boiler; and one or more pumps for regulating gas and / or liquid flow.

21. An apparatus according to claim 20 wherein the heat - exchanger comprises a 'tube-in-tube' heat-exchanger.

22. An apparatus according to any of claims 1 to 21 further comprising a means for regenerating boiler solution from the used solution formed within the boiler, said means comprising in sequence; a separator which receives used solution from the boiler; a steamer apparatus for boiling down used solution to a required concentration, said steamer apparatus being adapted to receive steam and including a heater and means for removing gases released from the boiling down of the used solution; and means for returning the regenerated solution from the steamer apparatus to the boiler.

23. An apparatus according to claim 22 wherein the steamer apparatus further includes a distribution device for distributing used solution received from the separator, and a series of parallel tubes.

24. An apparatus according to claim 23 in which the temperature inside the parallel tubes is different to that outside the parallel tubes.

25. An apparatus according to claims 22 to 24 wherein said means for returning the regenerated boiler solution to the boiler includes a tank for temporary storage of the solution.

26. An apparatus according to any of claims 22 to 25 wherein said means for returning the regenerated boiler solution to the boiler includes a vaporiser apparatus in which the used solution is further boiled down.

27. An apparatus according to claim 26 further comprising a cyclone which receives gases generated in the vaporiser and removes fibres of material supported within the gases.

28. An apparatus according to any of claims 1 to 27 further including means for treating fluids generated in the boiler, said means comprising two vaporisers, a cyclone for removing fibres supported in the gases entering the cyclone from the vaporisers, and a heat exchanger to condense the gases received from the cyclone.

29. An apparatus according to claim 28 whereby said means for treating fluids also receives gases generated in the unloader.

30. An apparatus according to claim 28 or 29 whereby said means for treating gases also receives gases generated in the fluffer.

31. An apparatus according to any of claims 28 to 30 whereby said means for treating gases also receives gases generated in the accumulation reservoir.

32. An apparatus according to any of claims 28 to 31 further including a tank which receives condensed liquid from the heat exchanger.

33. An apparatus according to any of claims 28 to 32 further comprising means for supplying gases not condensed in the heat exchanger to the first scrubber for use in the preparation of the boiler solution.

34. An apparatus according to any of claims 1 to 33 further including an emergency tank connected to the boiler through a blower tube.

35. An apparatus according to any of claims 1 to 34 further including a helper bunker into which pulp caught in the emergency tank or cyclones is unloaded.

36. An apparatus for the production of pulp from raw plant material as substantially described herein with reference to the accompanying drawings.