CN101408007A - Two vessel reactor system and method for hydrolysis and digestion of wood chips with chemical enhanced wash method - Google Patents
Two vessel reactor system and method for hydrolysis and digestion of wood chips with chemical enhanced wash method Download PDFInfo
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- CN101408007A CN101408007A CNA2008100977497A CN200810097749A CN101408007A CN 101408007 A CN101408007 A CN 101408007A CN A2008100977497 A CNA2008100977497 A CN A2008100977497A CN 200810097749 A CN200810097749 A CN 200810097749A CN 101408007 A CN101408007 A CN 101408007A
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Abstract
A reactor vessel system includes: a first reactor vessel having a hydrolysate and liquid extraction screen, a first region above the extraction screen that is maintained at conditions promoting a hydrolysis reaction in the cellulosic material, a second region below the extraction screen in which the hydrolysis is substantially suppressed and a wash liquid inlet below the extraction screen providing wash liquid at a temperature below a hydrolysis temperature; a transport pipe having an inlet coupled to the first reactor vessel and an outlet coupled to a second reactor vessel, and the second reactor vessel includes a liquid discharge that extracts a portion of liquid from the second reactor vessel and directs the portion of liquid to the first reactor vessel or to the transport pipe.
Description
The application requires the U.S. Provisional Application sequence number No.60/939 that submitted on May 23rd, 2007,718 rights and interests, and it incorporates this paper in full by reference into.
Technical field
The present invention relates to be used for the method and apparatus of cellulosic fibre material hydrolysis process.
Background technology
In legacy system, wood chip (or other celluloses or fibrous material) is hydrolyzed in first reactor vessel before second container such as boiling vessel for example being directed to.At United States Patent (USP) 4,174, in 997 (' 997 patents) a kind of such legacy system has been described.In first reactor vessel, the hydrolysis of the sawdust pulp of the described container of process is carried out under acid condition.In first reactor vessel, hydrolysate, for example sugar such as pentose and hexose extracts from wood chip, and the recycle-water hydrolysis products.Fibrous material is discharged from the bottom of described first reactor vessel, and is transported to the top of second reactor vessels such as boiling vessel for example by conveyance conduit, and the boiling that is used for cellulosic material is handled.
In traditional system, as describing in ' 997 patents, hydrolysis is carried out in whole first reactor vessel.Sawdust pulp is introduced the top of first reactor vessel, and discharges from the bottom of described container.By will be for example 150 degrees centigrade (℃) hot water be directed to container bottom, and steam is directed to container top container is heated.In addition, add acid solution and promote hydrolysis, especially under material is lower than 150 ℃ temperature.Hot water upwards flows in container, and it is reverse with the fibrous material that flows downward.Hot water and steam are kept hydrolysis in the entire container with enough heat supply materials.
In some legacy systems, the boiling chemicals, for example white liquid is incorporated into first reactor vessel bottom, and introduces the conveyance conduit that is used for sawdust pulp is transported to from first reactor vessel second reactor vessel.The boiling chemicals makes the fiber of the cellulosic material that begins to permeate first reactor vessel bottom to the injection of first reactor vessel bottom, but hydrolysis is still carrying out simultaneously.When the boiling chemicals is introduced cellulosic material, be hydrolyzed and do not expect.
Summary of the invention
Developed a kind of hydrolysis system that is used for pulping system of novelty.For example cellulosic material such as wood chip is hydrolyzed in the upper zone of first reactor vessel (hydrolysis reactor).The hydrolysis preferably material in container is under the temperature between 150 ℃ to about 175 ℃, more preferably carries out under the temperature between 160 ℃ to 170 ℃.The hydrolysis preferably material in container is in 1 to 6 pH value, and more preferably is under the situation of 3 to 4 pH value and carries out.Hydrolysate and liquid are removed from hydrolysis reactor by extracting sieve.
Below extracting sieve, upwards flow through scrubbing section in the hydrolysis reactor of cool cleaning solution arrives and extracts sieve.Cool cleaning solution suppresses to extract the hydrolysis in the following cellulosic material of sieve.Basically all hydrolysis are preferably carried out above the sieve of the extraction in hydrolysis reactor.Cool cleaning solution preferably has the temperature than low 10 ℃ to 70 ℃ of hydrolysis temperature, more preferably has the temperature than low 20 ℃ to 50 ℃ of hydrolysis temperature, most preferably has the temperature than low 25 ℃ to 35 ℃ of hydrolysis temperature.Cool cleaning solution preferably has 3 to 7 pH value, and most preferably has 4 to 5 pH value.And cool cleaning solution preferably mainly comprise water, and can comprise the chemicals of interpolation, and described amount of chemicals used is for example to flow through in the slurry of container 0.01% to 5% of cellulosic material amount such as timber.The amount of the chemicals that adds most preferably is 0.1% to 1% of cellulosic material amount in the slurry.The chemicals that adds in the cool washings can be any one or two kinds of of NaOH (NaOH) or the white liquid of essentially no sulphur, to prepare cool cleaning solution.
Developed a kind of reactor vessel system, comprise: first reactor vessel, have material input that receives cellulosic material and the material outlet side that is used for described cellulosic material, wherein, described cellulosic material arrives described material outlet side from described material input described first reactor vessel of flowing through; Hydrolysate in described first reactor vessel and liquid extraction sieve; First district of described first reactor vessel, between described material input and described liquid extraction sieve, wherein, described first district remains on the condition that promotes hydrolysis in the described cellulosic material; The heat energy input port is used for heated liquid is added to the described cellulosic material of described first district or described first district top; Second district of described first reactor vessel, between described liquid extraction sieve and described material outlet side, in described second district, described hydrolysis is suppressed basically; The cleaning solution ingress port is used for cleaning solution with below the described extraction sieve and described second district that flows through and is directed to described extraction and sieves, and wherein, described cleaning solution is introduced under the temperature of first hydrolysis temperature, and described cleaning solution suppresses the hydrolysis in described second district; Conveyance conduit, inlet with the described material outlet side that is attached to described first reactor vessel, with the outlet that is attached to second reactor vessel, wherein, described cellulosic material arrives described second reactor vessel from the described material outlet side described conveyance conduit of flowing through, and described second reactor vessel is applied to described cellulosic material in described second reactor vessel with cooked solution, and described second reactor vessel comprises the liquid outlet side, described liquid outlet side extracts a part of liquid from described second reactor vessel, and described partially liq is directed to the bottom inlet of described first reactor vessel or at least one in the described conveyance conduit.
A kind of flash tank can receive the liquid that extracts from the extraction sieve of described first reactor vessel, and above described first container area or described first container area steam is provided to described container.Described flash tank also can be discharged to hydrolysate the hydrolysate recovery system.
Developed a kind of reactor vessel system, comprise: first reactor vessel, has the top material input that receives cellulosic material, with the base material outlet side that is used for described cellulosic material, wherein, described cellulosic material arrives described material outlet side from described material input described first reactor vessel of flowing through; Hydrolysate in described first reactor vessel and liquid extraction sieve; The upper zone of described first reactor vessel, between described material input and described liquid extraction sieve, wherein, described upper zone remains on or is higher than hydrolysis temperature, and under described hydrolysis temperature, hydrolysis carries out in described cellulosic material; The heat energy input port is used for heated liquid is directed to the described cellulosic material of the upper zone of described first reactor vessel; The lower region of described first reactor vessel, between described liquid extraction sieve and described base material outlet side, in described lower region, described hydrolysis is suppressed basically; The cleaning solution ingress port, lower region at described first reactor vessel, be used for the cleaning solution of abundance is directed to described container, described lower region arrives described extraction sieve so that described cleaning solution is upwards flowed through, wherein, described cleaning solution is introduced under the temperature of the first described hydrolysis temperature, and described cleaning solution cooling and be suppressed at described hydrolysis in second district of described reactor vessel; Conveyance conduit, inlet with the described material outlet side that is attached to described first reactor vessel, with the outlet that is attached to described second reactor vessel, wherein, described cellulosic material arrives the upper entrance of described second reactor vessel from the described base material outlet side described conveyance conduit of flowing through, and described second reactor is applied to described cellulosic material in described second reactor vessel with cooked solution, and described second reactor vessel comprises the liquid outlet side, described liquid outlet side extracts solution from described second reactor vessel, and described partially liq is directed to the bottom inlet of described first reactor vessel or at least one in the described conveyance conduit.
Developed a kind of treatment system that is used for cellulosic material is transformed into paper pulp, described system comprises: the first pressurized reactor container, operate being higher than under the atmospheric pressure, described first reactor vessel comprises the material input that receives cellulosic material and is used for the material outlet side of described material, wherein, described cellulosic material flows to described material outlet side from described material input; The heat energy input port is on the top of described first reactor vessel; First district of described first reactor vessel, between described material input and liquid extraction sieve, wherein, described first district remains in the cellulosic material at least 170 degrees centigrade hydrolysis temperature; Described extraction sieve has the outlet that is used for extracting from described first container hydrolysate and liquid, second district with described first reactor, between described liquid extraction sieve and described outlet side, in described second district, temperature is lower than described hydrolysis temperature, and described hydrolysis reactor is suppressed basically, and the described first container outlet side below described second district; Described treatment system also comprises conveyance conduit, and flow-catheter is provided to continuous digestion container from described outlet side, and described continuous digestion container receives the described cellulosic material of discharging from described first reactor vessel.
Developed and a kind ofly prepared the method for paper pulp, having comprised: cellulosic material has been introduced upper entrance in first reactor vessel from cellulosic material; By increasing pressure and heat energy, with the described cellulosic material hydrolysis in the upper zone of described first reactor vessel to container; Extraction sieve below upper zone described in described first reactor vessel extracts hydrolysate from described cellulosic material; Cleaning solution is directed to the lower region of described first reactor vessel, and wherein said cleaning solution suppresses the hydrolysis of the cellulosic material in the described lower region, and the described cleaning solution described cellulosic material of upwards flowing through arrives described extraction sieve; Described cellulosic material is discharged from the lower part outlet of described first reactor vessel; Top with the cellulosic material of described discharge is directed to second reactor vessel and cooked solution is introduced described second reactor vessel prepares paper pulp with the described cellulosic material of digestion.
Developed a kind of method that suppresses the cellulosic material hydrolysis, having comprised: cellulosic material is directed in the upper entrance of first reactor vessel, wherein, described material moves downward through described container; To be higher than atmospheric steam and be increased to described first reactor vessel; Described cellulosic material in the upper zone of described first reactor vessel is kept above hydrolysis temperature; Extraction sieve below upper zone described in described first reactor vessel extracts hydrolysate from described cellulosic material; Described cellulosic material below the described extraction sieve is cooled to be lower than the temperature of described hydrolysis temperature and described cellulosic material is discharged from the outlet at bottom of described first reactor vessel.
Description of drawings
Fig. 1 is the schematic diagram with continuous pulping system of wood chip supply, hydrolysis reactor and continuous steamer reactor.
The specific embodiment
In the double-reactor containment system, steam is incorporated into the top of two containers for heating and pressurization purpose.Carry out above the extraction sieve of hydrolysis in the described first reactor vessel top.When the wood chip of introducing at the top of described first container or other celluloses or fibrous material (being generically and collectively referred to as cellulosic material) through described container and when arriving this container bottom and extracting port, the extraction sieve in described first reactor vessel is removed hydrolysate.
Described cellulosic material washs below described extraction sieve in first reactor vessel.Cleaning solution is introduced in the bottom of described first reactor vessel, and flows upward to described extraction sieve.Cleaning solution can be water or the water that mixes with one or more chemicalss, and described chemicals for example is the white liquid of NaOH (NaOH) and essentially no sulphur.The diameter of described first container can be with following consistent above described extraction sieve.The cellulosic material of discharging from the extraction port of described first reactor vessel is directed to the top of second reactor vessel, and described second reactor vessel can be a digester vessel.Cellulosic material boiling in second reactor vessel generates paper pulp, and described paper pulp extracts port from the bottom of described second reactor vessel and discharges.
In first reactor vessel, cellulosic material washs in the bottom of described container, to remove hydrolysate from described material.Washing in the bottom of described first container uses the cleaning solution under the temperature that is being lower than hydrolysis temperature to carry out.The cleaning solution temperature is preferably than low 10 ℃ to 70 ℃ of hydrolysis temperature, more preferably than low 20 ℃ to 50 ℃ of hydrolysis temperature, most preferably than low 25 ℃ to 35 ℃ of hydrolysis temperature.Cleaning solution is cooled to cellulosic material the temperature of normal hydrolysis temperature.Cool cleaning solution washes away remaining hydrolysate from cellulosic material, the temperature of cellulosic material be reduced to be lower than hydrolysis temperature, and with the pH value of the cellulosic material in first reactor vessel described material in second reactor vessel, be adjusted to before the boiling near or be higher than neutrality (the pH value is 7) a little.
Cool cleaning solution preferably has 3 to 7 pH value, and more preferably has 4 to 5 pH value.The pH value of cool cleaning solution is remained on the deposition that can prevent or be minimized in the lignin that dissolves in the boiling chemicals of second reactor vessel in these scopes.Cleaning solution can comprise the chemicals of interpolation, the white liquid of NaOH and essentially no sulphur for example, the amount of the hydrolysate that extracts with the cellulosic material that improves from first container.The deposition of lignin in first container can be reduced in the bottom that cleaning solution rather than a large amount of white liquid are introduced described first reactor vessel, if a large amount of white liquid adds the bottom of described first reactor vessel, the deposition of lignin in first container may take place then.
Second reactor vessel can be continuous boiling container, for example steam or vapor phase boiling vessel.The use of steam or vapor phase boiling vessel will be avoided forming operational issue in the second reactor vessel top of causing by the gas in hydrolytic process.First and second reactor vessels can be upright basically, has the outlet side of at least 100 feet height, the inlet in container top and close container bottom.The heat energy that is increased to reactor vessel can be in the pressurized vapor that is higher than under the atmospheric pressure.
Fig. 1 be have first reactor vessel 10 (hydrolysis reactor) and for example continuously the exemplary wood chip of second reactor vessel 12 of pulp digester supply with and the schematic diagram of pulp processing system.Described first reactor vessel comprises inverted top separator 14, fiber material slip and liquid that it receives from traditional wood chip feeding assembly 15 by wood chip service 33.
Wood chip feeding assembly 15 can comprise the wood chip cabin 16 that is connected to two screw wood chip chis 18 and wood chip skewed slot 20, and for example Andritz Inc. sells
The wood chip cabin.Hot water 24 adds wood chip or other cellulosic materials in the wood chip skewed slot 20 to by pipeline 26, to form the fiber material slip.Liquid allotment case 22 is fed to the wood chip pipe with water.Water also can directly be fed to the wood chip skewed slot by pipeline 23.
The separating liquid of discharging and extract pipeline 27 from top separator 14 can mix (referring to valve 25) with hot water.Flow through pipeline 26 of mixture arrives allotment casees 22, and arrives wood chip skewed slots 20 by pipeline 23.Use valve 25 to control to the normal hydrolysis temperature that is lower than cellulosic material, for example 170 ℃ temperature from the liquid of top separator 14 discharges and the mixture of hot water 24.The temperature of the water and the liquid of discharging from the top separator is the temperature 100 ℃ to 120 ℃ scopes preferably.By temporary transient storage of water with from the mixture of the solution of top separator, allotment case 22 can be used for being provided for forming the temperature control of the water and the liquid mixture of cellulose slurry.For example, temperature control can provide by regulating from top separator liquid and the relative quantity of hot water 24 the allotment case that pipeline 27 arrives the allotment casees of flowing through.
For wood chip being fed to first reactor vessel, (for example Andritz Inc. sells the fiber material slip by one or more pumps 32
System and United States Patent (USP) 5,752,075; 6,106,668; 6,325,890; 6,551,462; The pump of describing in 6,336,993 and 6,841,042) is pumped into the top separator 14 of first reactor vessel.Other starch feed system, for example use the feed system of high voltage supply device also can use.
Pressure from gas phase helps cellulosic fibre material is promoted downwards, and discharges from first container at first container bottom, 56 outlet sides.In first reactor vessel 10, potential pressure adds that hydrostatic head should be transported to second reactor vessel with the cellulosic material that helps to discharge from first reactor vessel than higher in second reactor vessel 12.If in second reactor vessel, potential pressure adds that static pressure is big first watch, then can use the wood chip pump that material is pumped into second container from first container between two containers.
Steam 72 is for example supplied with under 170 ℃ the temperature being higher than normal hydrolysis temperature, so that hydrolysis can be carried out in the cellulose slurry in first reactor vessel.Steam is so that small part promotes the control mode of hydrolysis in first reactor vessel to add.Steam passes through at the first reactor vessel top or the pipeline 74 of close first reactor head and 68 adds, thereby arrives the gas phase 45 of container.Introduce the steam of first reactor vessel temperature of cellulose slurry is brought up to normal hydrolysis temperature or is higher than normal hydrolysis temperature, for example be higher than 150 ℃.
The fiber material slip that is fed to inverted top separator 14 in first reactor vessel can have excessive liquid, is beneficial to flow through conveyance conduit 33.In case in container, then when starching through top separator 14, excessive liquid is removed.The excessive liquid of removing from separator turns back to the wood chip feed system by pipeline 27, for example turns back to wood chip skewed slot 20, and is directed to slurry once more, and cellulosic material is transported to first container top.Hot liquid can be in the top of first reactor vessel separator 14 and gas phase 45 places or close top separator 14 and gas phase 45 interpolations.The liquid that adds can be the hot liquid at hot water 24 (pipe-line system does not show) or 48 extractions of the sieve of the extraction from first reactor vessel and the pipeline 31 arrival first reactor vessel top of flowing through.
Hydrolysis is carried out in the upper zone 46 of first reactor vessel 10, and temperature remains on normal hydrolysis temperature or is higher than normal hydrolysis temperature in described first reactor vessel.By adding acid, hydrolysis will be carried out under lower temperature, for example be lower than 150 ℃, but only make water and from the circulating fluid of the first reactor vessel top separator, then selective hydrolysis is at high temperature carried out, and for example is higher than 150 ℃ to 170 ℃.Hydrolysis will be basically only being extracted above the sieve 48, or the extraction of one group of differing heights is sieved in the upper zone 46 of 48 tops and carried out.
When cellulosic material moves down by container 10, through extracting sieve at 48 o'clock, in order to stop hydrolysis, the temperature of material is reduced to and is lower than hydrolysis temperature, perhaps by extracting sieve 48 acid in the cellulosic material is removed from first reaction vessel.Reduce temperature and remove acid from cellulosic material and can use together or make separately and be used for suppressing and preferably stoping hydrolysis.
Hydrolysate is the product of hydrolysis.Hydrolysate is removed with cleaning solution and some other liquid together by extracting sieve 48, and is fed to pipeline 29, and flows to flash tank 30.Hydrolysate, cleaning solution and other extracts are recyclable or be recycled to the wood chip feed system.Liquid from first reactor vessel 10 that extract and the pipeline 29 that be directed to flash tank 30 comprises the hydrolysate that extracts from first reactor vessel.Flash tank 30 draws liquid with hydrolysate to be separated from steam.Liquid from flash tank preferably is being lower than under the temperature of hydrolysis temperature, and more preferably less than 110 ℃.Liquid with hydrolysate flows to pipeline 28 from flash tank, and steam can turn back to the upper gaseous phase of first reactor vessel 10 by pipeline 68.Part hydrolysate reclaims by traditional hydrolysate recovery system 70.
Steam 68 can be introduced container, if the pressure particularly in the container is lower than the pressure in the flash tank.If the pressure of container is not less than flash tank, then steam is bootable to the wood chip cabin, the heater that is used for water and/or white liquid that uses in this process.United States Patent (USP) 7,105,106 and U.S. Patent Publication thing 2007-0000626 in the similar cycle of steam and/or extract has been described.
From the liquid of flash tank 30, comprise a part of hydrolysate, the pipeline 28,71 of flowing through arrives the sawdust pulp in the wood chip skewed slot 20, and via pipeline 73, arrives liquid allotment case 22.Add in the wood chip skewed slot 20 amount of liquid with hydrolysate of sawdust pulp to and can control the too much change of avoiding sawdust pulp pH value, for example, avoid making slurry to become and too be alkalescence or too be acid.Liquid helps the sawdust pulp material is carried by wood chip pump 32 and by the sawdust pulp pipeline 33 that extends between the top separator 14 of the wood chip skewed slot 20 and first reactor vessel 10 to being added with of cellulosic material in the wood chip skewed slot 20.
Before being directed to container 10 bottoms, chemicals 82, the white liquid of NaOH or essentially no sulphur for example can add the cool washings of the pipeline 52 of flowing through by pipeline 84 to.The amount of adding the chemicals in the cleaning solution to can be the cellulosic material in the slurry of container of flowing through, for example 0.01% of the amount of timber to 5%.The amount of chemicals used of adding is preferably 0.1% to 1% of cellulosic material.Chemicals adds washings to be suppressed hydrolysis and removes hydrolysate, and the pH value of regulating cleaning solution alternatively.If cleaning solution is a pure water, then such phenomenon can occur: chemicals adds washings to and causes more basically hydrolysate to extract from the cellulosic material of the scrubbing section of flowing through.
When in cleaning solution 50 and the scrubbing section and extracting sieve 48 places or above cellulosic material when interacting, described liquid is cooled to be lower than hydrolysis temperature with cellulosic material, and some chemical materials are washed out from described material.Preferably, cool cleaning solution reduction extraction is sieved near 48 and the temperature of the cellulosic material in the scrubbing section 54, with the hydrolysis in inhibition and the prevention material.In addition, when the cellulosic material of hydrolysis moves to when extracting below the sieve 48, preferred described material is in the undissolved pH value of lignin level.Amount of chemicals used in cleaning solution and the cleaning solution can make the pH value level of the cellulosic material in the scrubbing section 54 be adjusted in the predetermined pH value scope.
Discharge the bottom 56 of the wood chip of washing by first reactor vessel, and be sent to the top separator 57 of second reactor vessel 12 by wood chip conveyance conduit 62, for example inverted top separator, and described second reactor vessel 12 for example is a continuous steamer.Pump 64 is used for auxiliary from first reactor vessel cellulosic material being transported to second reactor vessel by pipeline 62 alternatively.Residual water and other liquid can be used for increasing the ratio of liquid and wood chip in the cellulosic material of pipeline 62 of flowing through in the wood chip, helping by the described material of pipeline 60 conveyings, and are transported to the top separator 56 of second reactor vessel.
Can add fiber material slip in the conveyance conduit 62, the bottom of perhaps adding first reactor vessel to from other liquid of pipeline 58 by pipeline 61.Described other liquid can extract from the top separator 57 of second reactor vessel 12.Described other liquid can and be recycled to the bottom 56 of first container by pumping (by pump 59) via pipeline 58 and 61.Liquid in the pipeline 58 can directly be directed in the exhaust steam of the cellulosic material in the pipeline 62, perhaps is directed to the bottom 56 of first reactor vessel via pipeline 61, as being used for a part of liquid that auxiliary wood chip is discharged from first container.Valve 63 is directed to pipeline 61 or conveyance conduit 62 with liquid stream from pump 59 and pipeline 58.To not have basic matterial comparatively speaking from the liquid of top separator 57 recirculation of second container, and the control of pH value can be regulated and guarantees that recycled liquid had acceptable pH value level before bottom of introducing first reactor vessel 10 or conveyance conduit 62.
Acid can be added the circulating line 62 auxiliary pH value controls that are transported to the cellulosic material of second reactor vessel from first reactor vessel to.If the pH value of the cellulosic material in the wood chip conveyance conduit 62 on the pH value level of expectation, is then added to the acidic chemical medicine in the pipeline 62 or the bottom 56 of adding first reactor vessel to can be used for reducing pH value in the cellulosic material.
PH value watch-dog 78 can be used for sensing flows to the cellulosic material of second reactor vessel from first reactor vessel pH value level.If watch-dog 78 detects the pH value scope that pH value level in the cellulosic material is higher than expectation, then controller can make the acidic chemical medicine add cellulosic material in the bottom 56 of first container 10 or in conveyance conduit 62 to.In addition, if watch-dog 78 detects the pH value scope that pH value level is higher than expectation, then controller can make other washings introduce the bottom 56 of first container or be directed to pipeline 62.
Can be used for heat is increased to any of wood chip feed system 16, first reactor vessel and heat recovery system 90 via pipeline 68 from the steam of flash tank 30,66.For example, the steam that extracts from first reactor vessel 10 rises to wood chip cabin 16 and comes Assisted Preparation fiber material slip, and is used for controlling the ratio of slurry liquid to timber.Before steam is increased to the wood chip feed system, can check that steam determines its essentially no sulphur.Preferably, the chemicals of sulfur-bearing does not add cellulosic material to or adds any other material or the liquid of introducing first reactor vessel 10 to.Sulphur in first reactor vessel 10 may disadvantageously form the sulphur compound of container 10,12 neutralizations from the liquid that extracts sieve 48 extractions.
The boiling chemicals, for example, white liquid 76, the top of adding second reactor vessel 12 to is for example added and is led inverted top separator 57.The part of these boiling chemicalss is bootable to extracting solution from top separator 57 and adding liquid the bottom of first reactor vessel to or add the circulating line 58 of wood chip conveyance conduit 62 to.White liquid 76 adds the top separator of second reactor vessel 12 to, promoting mixing of solution and cellulosic material in the separator, and carries out before the mixture of material and solution is discharged to second reactor vessel from separator.
The monitoring of circulating line 58 comprises pH value watch-dog, may be to determining that the boiling chemicals does not flow to first reactor vessel 10 or flows to conveyance conduit 62 of great use from second reactor vessel 12.PH value in the circulating line 58 will remain in the scope of pH value 4 to pH values 10, preferably remain in 6 to 10 the scope, more preferably remain in 6 to 8 the scope.If the pH value in the circulating line 58 is high, then other cool washings 50 can add the bottom 56 of first reactor vessel to or add conveyance conduit 62 to.Washings 50 can add the bottom of first reactor vessel to or add the conveyance conduit 62 auxiliary tops of the fiber material slip being shifted onto second reactor vessel from first container to.
Though the present invention is described about being considered to the most practical and preferred embodiment at present, it should be understood that, the present invention arrives the disclosed embodiments without limits, but opposite, is intended to cover various improvement and equivalent arrangements included in the spirit and scope of the appended claims.
Claims (56)
1. reactor vessel system comprises:
First reactor vessel has material input that receives cellulosic material and the material outlet side that is used for described cellulosic material, and wherein, described cellulosic material arrives described material outlet side from described material input described first reactor vessel of flowing through;
Hydrolysate in described first reactor vessel and liquid extraction sieve;
First district of described first reactor vessel, between described material input and described liquid extraction sieve, wherein, described first district remains on the condition that promotes hydrolysis in the described cellulosic material;
Second district of described first reactor vessel, between described liquid extraction sieve and described material outlet side, in described second district, described hydrolysis is suppressed basically;
The cleaning solution ingress port is used for cleaning solution with below the described extraction sieve and described second district that flows through and is directed to described extraction and sieves, and wherein, described cleaning solution is introduced under the temperature of first hydrolysis temperature, and described cleaning solution suppresses the hydrolysis in described second district;
Conveyance conduit, have the inlet of the described material outlet side that is attached to described first reactor vessel and be attached to the outlet of second reactor vessel, wherein, described cellulosic material arrives described second reactor vessel from the described material outlet side described conveyance conduit of flowing through, and
Described second reactor vessel is applied to described cellulosic material in described second reactor vessel with cooked solution, and described second reactor vessel comprises the liquid outlet side, described liquid outlet side extracts a part of liquid from described second reactor vessel, and described partially liq is directed to the bottom inlet of described first reactor vessel or at least one in the described conveyance conduit, and
Wherein, described cleaning solution is the mixture of at least a and water in NaOH and the white liquid of essentially no sulphur.
2. reactor vessel according to claim 1 system, wherein, in 0.01% to 5% scope of the described at least a described cellulosic material amount at the described container of flowing through in NaOH and the white liquid of essentially no sulphur.
3. reactor vessel according to claim 1 system wherein, carries out in described container under the temperature of hydrolysis in 150 ℃ to 175 ℃ scopes.
4. reactor vessel according to claim 1 system, wherein, described hydrolysis is carried out in described container in 1 to 6 pH scope.
5. reactor vessel according to claim 3 system, wherein, described cleaning solution is lower 10 ℃ to 70 ℃ than described hydrolysis temperature.
6. reactor vessel according to claim 1 system, wherein, described cleaning solution has the pH value in 3 to 7 scopes.
7. reactor vessel according to claim 1 system also is included in the top separator in described second reactor vessel, and the liquid of described extraction part is extracted from described top separator.
8. reactor vessel according to claim 1 system also comprises the pH value watch-dog of fiber material slip pH value level described in the described conveyance conduit of monitoring.
9. reactor vessel according to claim 1 system also comprises flash tank, receives the liquid that extracts from described extraction sieve, and above described first container area or described first container area steam is provided to described first reactor vessel.
10. reactor vessel according to claim 9 system, wherein, described flash tank has the liquid outlet side, and described liquid outlet side provides liquid for the wood chip feeding assembly of described system.
11. a reactor vessel system comprises:
First reactor vessel, has the top material input that receives cellulosic material, with the base material outlet side that is used for described cellulosic material, wherein, described cellulosic material arrives described material outlet side from described material input described first reactor vessel of flowing through;
Hydrolysate in described first reactor vessel and liquid extraction sieve;
The upper zone of described first reactor vessel, between described material input and described liquid extraction sieve, wherein, described upper zone remains on or is higher than hydrolysis temperature, and under described hydrolysis temperature, hydrolysis carries out in described cellulosic material;
The heat energy input port is used for heated liquid is directed to the described cellulosic material of the upper zone of described first reactor vessel;
The lower region of described first reactor vessel, between described liquid extraction sieve and described base material outlet side, in described lower region, described hydrolysis is suppressed basically;
The cleaning solution ingress port, lower region at described first reactor vessel, be used for the cleaning solution of abundance is directed to described container, described lower region arrives described extraction sieve thereby described cleaning solution is upwards flowed through, wherein, described cleaning solution is introduced being lower than under the temperature of described hydrolysis temperature, and described cleaning solution cooling and be suppressed at described hydrolysis in the lower region of described reactor vessel;
Conveyance conduit, inlet with the described material outlet side that is attached to described first reactor vessel, with the outlet that is attached to described second reactor vessel, wherein, described cellulosic material arrives the upper entrance of described second reactor vessel from the described base material outlet side described conveyance conduit of flowing through, and
Described second reactor vessel comprises the cooked solution that is applied to described cellulosic material, and described second reactor vessel comprises the liquid outlet side, described liquid outlet side extracts solution from described second reactor vessel, and described partially liq is directed to the bottom inlet of described first reactor vessel or at least one in the described conveyance conduit, and
Wherein, described cleaning solution is the mixture of at least a and water in NaOH and the white liquid of essentially no sulphur.
12. reactor vessel according to claim 11 system, wherein, in 0.01% to 5% the scope of the described at least a described cellulosic material amount at the described container of flowing through in NaOH and the white liquid of essentially no sulphur.
13. reactor vessel according to claim 11 system wherein, carries out in described container under the hydrolysis temperature of hydrolysis in 150 ℃ to 175 ℃ scopes.
14. reactor vessel according to claim 11 system, wherein, hydrolysis is carried out in the pH value is 1 to 6 scope.
15. reactor vessel according to claim 11 system, wherein, described cleaning solution is lower 10 ℃ to 70 ℃ than described hydrolysis temperature.
16. reactor vessel according to claim 11 system, wherein, described cleaning solution has the pH value in 3 to 7 scopes.
17. reactor vessel according to claim 11 system also is included in the top separator in described second reactor vessel, and the liquid of described extraction part is extracted from described top separator.
18. reactor vessel according to claim 11 system also comprises the pH value watch-dog that monitors fiber material slip pH value level described in the described conveyance conduit.
19. reactor vessel according to claim 11 system also comprises flash tank, receives the liquid that extracts from described extraction sieve, and steam is provided to described first reactor vessel above described first container area or described first container area.
20. reactor vessel according to claim 19 system, wherein, described flash tank has the liquid outlet side, and described liquid outlet side provides liquid for the wood chip feeding assembly of described system.
21. a treatment system is used for changing cellulosic material into paper pulp, described system comprises:
The first pressurized reactor container is operated being higher than under the atmospheric pressure, and described first reactor vessel comprises:
Receive the material input and the material outlet side that is used for described material of cellulosic material, wherein, described cellulosic material flows to described material outlet side from described material input;
The heat energy input port is on the top of described first reactor vessel;
First district of described first reactor vessel, between described material input and liquid extraction sieve, wherein, described first district remains in the cellulosic material at least 150 degrees centigrade hydrolysis temperature;
Described extraction sieve have be used for from described first container extract hydrolysate and liquid outlet and
Second district of described first reactor, between described liquid extraction sieve and described outlet side, in described second district, temperature is lower than described hydrolysis temperature, and described hydrolysis reactor is suppressed basically and
The outlet side of described first container below described second district;
Conveyance conduit, with flow-catheter from described outlet side be provided to continuous digestion container and
Described continuous digestion container receives the described cellulosic material of discharging from described first reactor vessel.
22. treatment system according to claim 21, also comprise the cleaning solution input, be input to the described first pressurized reactor container, and below described extraction sieve, wherein, described cleaning solution input is connected to washer fluid source, and described cleaning solution comprises at least a in NaOH and the white liquid of essentially no sulphur, and at least a amount in NaOH and the white liquid of essentially no sulphur is in 0.01% to 5% scope of the described cellulosic material amount of the described container of flowing through.
23. treatment system according to claim 21, wherein, described cleaning solution has the pH value in 3 to 7 scopes.
24. treatment system according to claim 21, wherein, described hydrolysis temperature is in 150 ℃ to 175 ℃ scopes.
25. treatment system according to claim 21, wherein, the cellulosic material in described first district in described first reactor vessel has the pH value in 1 to 6 scope.
26. treatment system according to claim 21, wherein, the temperature in described second district of described first reactor is in the scope than low 10 ℃ to 70 ℃ of described hydrolysis temperature.
27. treatment system according to claim 21, wherein, described first reactor vessel is vertical substantially, has at least 100 feet height, and described inlet is in the top of described container, and described outlet side is near the bottom of described container.
28. treatment system according to claim 21, wherein, the described heat energy input port of described first reactor vessel receives and is higher than atmospheric steam.
29. treatment system according to claim 21, also comprise flash tank, the liquid that reception is extracted from described extraction sieve at described first container area or be higher than described first container area and be provided to described first reactor vessel, and is discharged to the hydrolysate recovery system with hydrolysate with steam.
30. treatment system according to claim 29, the cleaning solution that also is included in bottom, described second district enters the mouth, and wherein, described cleaning solution inlet is attached to cool washer fluid source.
31. treatment system according to claim 21, wherein, described washer fluid source comprises at least a source and the cool washer fluid source in NaOH and the white liquid of essentially no sulphur, and wherein, the amount of described NaOH and the white liquid of essentially no sulphur is no more than 5% percent by volume of water in the cleaning solution.
32. one kind prepares the method for paper pulp from cellulosic material, comprising:
Cellulosic material is introduced upper entrance in first reactor vessel;
By increasing pressure and heat energy, with the described cellulosic material hydrolysis in the upper zone of described first reactor vessel to container;
Extract hydrolysate from the described cellulosic material of the sieve of the extraction below upper zone described in described first reactor vessel;
Cleaning solution is directed to the lower region of described first reactor vessel, and wherein said cleaning solution suppresses the hydrolysis of the cellulosic material in the described lower region, and the described cleaning solution described cellulosic material of upwards flowing through arrives described extraction sieve;
Described cellulosic material is discharged from the lower part outlet of described first reactor vessel;
With the cellulosic material of described discharge be directed to second reactor vessel and
Top with cooked solution is introduced described second reactor vessel prepares paper pulp with the described cellulosic material of digestion.
33. method according to claim 32, wherein, described cleaning solution comprises at least a of a certain amount of NaOH and the white liquid of essentially no sulphur, and described amount is in 0.01% to 5% scope of the cellulosic material amount of described first reactor vessel of flowing through.
34. method according to claim 32 wherein, is carried out under the hydrolysis temperature of described hydrolysis in 150 ℃ to 175 ℃ scopes.
35. method according to claim 34, wherein, described cleaning solution is lower 10 ℃ to 70 ℃ than described hydrolysis temperature.
36. method according to claim 32, wherein, described hydrolysis is carried out when described cellulosic material has pH value in 1 to 6 scope.
37. method according to claim 32, wherein, described cleaning solution has the pH value in 3 to 7 scopes.
38. method according to claim 32, wherein, described cellulosic material in the described upper zone remains on the temperature that is higher than hydrolysis temperature, and with the promotion hydrolysis, and the described cellulosic material in the described lower region remains below the temperature of at least 10 degrees centigrade of described hydrolysis temperatures.
39. according to the described method of claim 38, wherein, described hydrolysis temperature is at least 170 degrees centigrade.
40. method according to claim 32 also comprises from the described second reactor vessel extracting liq and the liquid of described extraction is introduced the lower region of described first reactor vessel.
41. according to the described method of claim 40, also comprise the pH value of monitoring described extraction solution, and if the pH value of described monitoring surpass predetermined pH value level, then be increased to the flow of liquor of described lower region.
42. method according to claim 32 also comprises steam is increased to described first reactor vessel to increase heat energy with described container pressurization with to described container.
43. method according to claim 32, wherein, described cleaning solution is the mixture of at least a and water in NaOH and the white liquid of essentially no sulphur, and wherein, the amount of described NaOH and white liquid is no more than 5% percent by volume of the described water in the described cleaning solution.
44. a method that suppresses the cellulosic material hydrolysis comprises:
Cellulosic material is directed in the upper entrance of first reactor vessel, wherein, described material moves downward through described container;
To be higher than atmospheric steam and be increased to described first reactor vessel;
Described cellulosic material in the upper zone of described first reactor vessel is kept above hydrolysis temperature;
From the described cellulosic material of the sieve of the extraction below upper zone described in described first reactor vessel, extract hydrolysate;
With the described cellulosic material below the described extraction sieve be cooled to be lower than described hydrolysis temperature temperature and
Described cellulosic material is discharged from the outlet at bottom of described first reactor vessel.
45. according to the described reactor vessel of claim 44 system, wherein, described cooling step is included in the following cleaning solution that adds of described extraction sieve, and described cleaning solution comprises at least a in a certain amount of NaOH and the white liquid of essentially no sulphur, and described amount is in 0.01% to 5% scope of the described amount of the cellulosic material of described first reactor vessel of flowing through.
46. according to the described reactor vessel of claim 44 system, wherein, described hydrolysis temperature is in 150 ℃ to 175 ℃ scope.
47. according to the described reactor vessel of claim 46 system, wherein, described cooling step is included in described extraction sieve and below cleaning solution is added to described first reactor vessel, wherein, described cleaning solution is lower 10 ℃ to 70 ℃ than described hydrolysis temperature.
48. according to the described reactor vessel of claim 46 system, wherein, described cleaning solution has the pH value in 3 to 7 scopes.
49. according to the described reactor vessel of claim 44 system, wherein, it is 1 to carry out in 6 the time that described hydrolysing step is in pH value scope at described cellulosic material.
50. according to the described method of claim 44, wherein, cool off described cellulosic material and comprise the lower region that cleaning solution is directed to described first reactor vessel, and make the described extraction sieve of the upwards mobile arrival of described cleaning solution.
51. according to the described method of claim 44, wherein, described cleaning solution is the mixture of at least a and water of NaOH and the white liquid of essentially no sulphur.
52. according to the described method of claim 44, wherein, the amount of described NaOH and white liquid is no more than 5% percent by volume of the described water in the described cleaning solution.
53. according to the described method of claim 44, wherein, described hydrolysis temperature is at least 170 degrees centigrade.
54. according to the described method of claim 44, comprise that also the described cellulosic material of will discharge from the outlet at bottom of described first reactor vessel is directed to the inlet that leads to second reactor vessel, extract appearance liquid from described second reactor vessel, and the solution of described extraction is directed to the lower region of described first reactor vessel.
55. according to the described method of claim 54, also comprise the pH value of monitoring described extraction solution, and if the pH value of being monitored surpass predetermined pH value level, then increase flow of liquor to described lower region.
56., also comprise steam is increased to described first reactor vessel to increase heat energy with described container pressurization with to described container according to the described method of claim 44.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510624388.7A CN105350368A (en) | 2007-05-23 | 2008-05-23 | Two vessel reactor system and method for hydrolysis and digestion of wood chips with chemical enhanced wash method |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US93971807P | 2007-05-23 | 2007-05-23 | |
| US60/939,718 | 2007-05-23 | ||
| US12/114,856 | 2008-05-05 |
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| CN201510624388.7A Division CN105350368A (en) | 2007-05-23 | 2008-05-23 | Two vessel reactor system and method for hydrolysis and digestion of wood chips with chemical enhanced wash method |
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| ZA (1) | ZA200803991B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103534407A (en) * | 2011-04-08 | 2014-01-22 | 百达工程建设私人有限公司 | Method and system for efficient production of dissolving pulp in a kraft mill producing paper grade pulp with a continuous type digester |
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2008
- 2008-05-09 ZA ZA200803991A patent/ZA200803991B/en unknown
- 2008-05-23 CN CNA2008100977497A patent/CN101408007A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103534407A (en) * | 2011-04-08 | 2014-01-22 | 百达工程建设私人有限公司 | Method and system for efficient production of dissolving pulp in a kraft mill producing paper grade pulp with a continuous type digester |
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| ZA200803991B (en) | 2009-03-25 |
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