Method for generation of clean steam in a continous digester system

Abstract

The invention relates to an improved method for generating clean steam in a digester plant of a chemical pulp mill. By feeding a steam-to-steam converter (SSC) with venting steam from a black liquor flash tank (FT) as well as venting steam from chip steaming (SV) could the volume of clean steam produced be increased by over 40-50%, and to such an extent that the volume of clean steam covers the needs for preheating of chips in the digester system also in severe operational conditions. The total consumption of clean steam from the steam net of the mill may be reduced and used for other purposes such as electricity production, which meets the requirements for converting the pulp mill to an environmental friendly pulp mill.

Claims

1. A method for generation of clean steam in a continuous digester system, where the continuous digester system comprises a chip bin using clean steam for an initial steaming of a cellulose material fed to the chip bin in order to heat the cellulose material and reduce an amount of air in a flow of the cellulose material; a steaming vessel using dirty steam for a subsequent steaming of the cellulose material fed to the steaming vessel wherein a stream of vent gases are withdrawn from the steaming vessel containing at least a part of bound air in the cellulose material fed to the steaming vessel; a path and liquor connection for slurrying the cellulose material that has been steamed in the steaming vessel to form a concentration of solids in a slurry; a feeder for transferring and pressurizing the slurry to a top of at least one treatment vessel, wherein at least one zone of the at least one treatment vessel contains a cooking zone kept at full cooking temperature, said full cooking temperature kept in the range 135 to 175 C.; an extraction screen in, or immediately following the cooking zone, extracting at least a spent cooking liquor kept at temperature in a range from 120 to 175 C. to form an extracted spent cooking liquor; at least one flash tank in a series of flash tanks for receiving the extracted spent cooking liquor, wherein the at least one flash tank reduces the pressure of the extracted spent cooking liquor and generates dirty flash steam from the extracted spent cooking liquor; the method comprising: leading the dirty flash steam as well as the stream of vent gases from the steaming vessel to a common steam-to-steam converter; and evaporating a clean steam from clean water fed to the steam-to-steam converter by indirect heating from the dirty flash steam as well as the stream of vent gases from the steaming vessel.

2. The method according to claim 1, wherein the amount of steam in the stream of vent gases from the steaming vessel fed to the common steam-to-steam converter exceeds 0.10 ton of steam per ton of air dried cellulose material fed to the digester system.

3. The method according to claim 2, wherein the amount of steam in the dirty flash steam fed to the common steam-to-steam converter exceeds 0.15 ton of steam per ton of air dried cellulose material fed to the digester system.

4. The method according to claim 3, wherein the temperature of the stream of vent gases from the steaming vessel is at least 110 C. and the temperature of the dirty flash steam is at least 105 C.

5. The method according to claim 4, wherein a stream of vent gases from the chip bin is led to the common steam-to-steam converter.

6. The method according to claim 1, wherein the stream of vent gases from the steaming vessel as well as the dirty flash steam from the flash tanks are mixed into one common flow of dirty steam laden gases before being fed to the common steam-to-steam converter.

7. The method according to claim 5, wherein the stream of vent gases from the chip bin is forwarded and led to and through the common steam-to-steam converter in a separate ducting system keeping the vent gases from the chip bin unmixed through the common steam-to-steam converter.

8. The method according to claim 1, wherein, after passage of the steam-to-steam converter, at least remnant steam flows from the stream of vent gases from the steaming vessel as well as the dirty flash steam from the flash tanks are led to a condenser for condensing remnant condensable gases, and after passage through the condenser the remnant gases are led to final incineration for destruction of non-condensable gases.

9. The method according to claim 7, wherein, after passage of the steam-to-steam converter, at least turpentine is extracted from remnant steam flow from the stream of vent gases from the chip bin.

10. The method according to claim 9, wherein the remnant steam flow from the stream of vent gases from the chip bin is subjected to further cooling.

Description

SUMMARY OF THE DRAWINGS

(1) FIG. 1 shows schematically a conventional 2-vessel digester system;

(2) FIG. 2 shows a modification of a conventional 2-vessel digester system where a reboiler is used;

(3) FIG. 3 shows the principle application of a steam-to-steam converter according to the invention in similar 2-vessel digester system;

(4) FIG. 4 show detail flow data for the steam-to-steam converter for a digester system with a production capacity of 1180 adt/day.

DETAILED DESCRIPTION

(5) FIG. 1 illustrates schematically a conventional 2-vessel digester system.

(6) The cellulose material, preferably in form of wood chips, flows to a chip bin CB via a chip meter. In many chips bins the chips are pre-steamed already in chip bin. This pre-steaming results in reduction of the most part of the free air in the chips flow but also a small part of the air bound in chips, as well as an initial heating of chips. Most often is flash steam used in the chip bin, but some chip bins use only clean steam from the steam net. The flash steam is typically obtained from a second flash tank FT.sub.2. Steaming in chip bin may be done in blow through fashion where clean steam is added in bottom and expelled in top. Steaming may also be done using dirty steam without blow trough of steam, and instead used cold top control of steam addition in bottom.

(7) After the chip bin is the chips steamed in a conventional pressurized steaming vessel SV, and a low pressure sluice feeder in inlet is used to enable application of higher pressure and thus higher temperature in the steaming vessel. This steaming phase is used to further reduce the amount of air bound in the chips. There is a vent in the steaming vessel and a degassing flow is sent to condensation system. In most conventional systems is flash steam from a first flash tank FT.sub.1 used for steaming in steaming vessel.

(8) Once the steaming is concluded and most of the air bound in the cellulose material has been driven off, the chips fall down in a chute where cooking liquor is added forming a slurry of chips. The chip slurry is sent to the top of a treatment vessel, here an impregnation vessel IV, using either a conventional high pressure sluice feeder, or as indicated here with a pump. Excess transport liquor is separated in top of the impregnation vessel and returned to chute. After impregnation, the chips slurry is sent to top of a digester vessel D where cooking and delignification takes place at full digester temperature in the range 140-180. In order to reach full digester temperature must heating be done in digester top, which may be done by injecting direct steam from the steam net of the mill into the digester top.

(9) At end of cook is spent cooking liquor at full cooking temperature, or lowest at 120 C., extracted via extraction screens and sent to a series of flash tanks FT.sub.1 and FT.sub.2 where the hot spent liquor flash off steam. Finally at end of digester is the cooked cellulose pulp P.sub.OUT fed out from digester.

(10) As shown in this figure was the steam partly reused in the system as the flash steam from the first flash tank was used for steaming in the steaming vessel, and flash steam was still used for steaming in chip bin, as there could be risks for blow through of malodourous gases, and flash steam from the second flash tank was used for heating towards full cooking temperature. Usage of direct steam for heating to cooking temperature, mostly for steam phase digesters, is the less expensive investment, but lead to dilution of cooking liquor with absolutely clean steam condensate and involves higher operational costs for generating replacement water with the same purity in the steam net.

(11) FIG. 2 illustrates schematically an improvement of the conventional 2-vessel digester system, but using a reboiler for generation of clean steam. The hot spent cooking liquor is sent to the reboiler REB, typically a kettle reboiler, where it indirectly heats a pool of clean water W fed to reboiler and driving off clean steam via outlet flow A. The clean steam CS produced could be used for the steaming process of the chips, as shown in U.S. Pat. No. 6,306,252. If more steam was needed could also the reboiler be put under lower pressure using an steam driven educator, as shown in U.S. Pat. No. 6,176,971, but then at the expense of clean steam and dilution effects. Indirect heating in digester top is used in a digester circulation sent to an indirect heat exchanger, and steam from the steam net may be used without dilution effects as the steam condensate is recovered separately.

(12) In FIG. 3 is a modification of the steam recovery system in similar 2-vessel digester system according to the invention. Here is a steam-to-steam converter SSC installed and being fed by both flash steam from a flash tank FT.sub.2 as well as vent steam from steaming vessel SV, collected at B. And the converted clean steam is obtained at X and used for steaming the chips. As shown here may only clean steam from the steam net of the mill be used to heat the digester top to full cooking temperature, which may be implemented as shown as a heating circulation in the top of an hydraulic digester or alternatively as steam addition to the vapor phase in a vapor phase digester. The function of the steam-to-steam converter will be more described in detail in FIG. 4 using the implementation data for a digester system with a production capacity of pulp at about 1180 adt/day. (adt=air dried ton, where 1 ton of air dried ton corresponds to 0.9 ton of bone dry ton). Thus, this production capacity is quite low today and corresponds to top production capacity in the early 1970ies, while production capacity of today may exceed 6000 adt/day. But numerous digesters from the 1970ies are still in operation and are subject to steam economy improvements.

(13) Example of Implementation

(14) As shown from the design data as disclosed in FIG. 4 has the steam-to-steam converter SSC a total heat exchange area of 1093 m.sup.2, with a K value of 1800 W/(m.sup.2* C.) and a delta T of about 6.2 C. There is also a small preheater PH used to heat fresh clean replacement water, with a total heat exchange area of 19.8 m.sup.2, with a K value of 1835 W/(m.sup.2* C.) and a delta T of about 10.4 C.

(15) The dirty side of the steam-to-steam converter SSC is fed with steam from the flash tank FT at an amount of 0.26 ton/adt of pulp produced, at a heat value of 2695.8 kJ/kg and in a volume of 1.09 m.sup.3/kg. The flash steam is forwarded in a piping with diameter of 500 mm, at a rate of 19.7 m/s and 12.8 ton/h (3.6 kg/s). The dirty side of the steam-to-steam converter SSC is also fed with steam from the steaming vessel SV at an amount of 0.15 ton/adt of pulp produced, at a heat value of 2711.1 kJ/kg and in a volume of 0.80 m.sup.3/kg. The vent steam from steaming is forwarded in a piping with diameter of 300 mm, at a rate of 23.2 m/s and 7.4 ton/h (2.0 kg/s). A small blow trough of about 5% is ventilated from the dirty side and sent to condenser, and this flow is forwarded in a piping with diameter of 200 mm, at a rate of 11.9 m/s and 0.3 kg/s. Dirty condensate is bled off at a rate of about 5% to a preheater PE, and this flow is forwarded in a piping with diameter of 80 mm, at a rate of 1.1 m/s and 5.3 l/s.

(16) The clean side of the steam-to-steam converter SSC is supplied with clean water (or condensate) and is under constant circulation by a circulation pump CP, withdrawing hot water from bottom of SSC and adding it to the top, flushing hot water over the heat exchanger surface. The clean steam is extracted from the lower part of the SSC behind a deflector skirt, and the amount of clean steam is generated in amount of 0.39 ton/adt of pulp produced, at a heat value of 2686.7 kJ/kg and in a volume of 1.34 m.sup.3/kg. The clean steam is forwarded in a piping with diameter of 700 mm, at a rate of 18.4 m/s and 19.1 ton/h (5.3 kg/s). The clean steam holds a pressure of about 30 kPa and a temperature of 106.9 C. As steam is continuously boiled off from the circulation is fresh clean water added to replace it, and in this example is the replacement water first heated in the pre heater PE using the residual heat value of the dirty condensate. The fresh water added is holding a temperature of about 80 C., and after heating in PE reach a temperature of about 96.1 C., and is added in a piping with diameter of 80 mm, at a rate of 1.1 m/s and 5.3 l/s. The preheated replacement water is preferably added directly into the circulation (using level control for controlling the supply). A small volume of is bled off from the circulation at a rate of about 5%, and this flow is forwarded in a piping with diameter of 25 mm, at a rate of 0.3 l/s and 0.6 m/s.

(17) Compared with feeding the steam-to-steam converter with only flash steam, the amount of clean steam generated increased from 0.25 ton/adt to 0.39 ton/adt, which corresponds to an increase of 0.14 ton/adt, i.e. 56%. The investment of a steam-to-steam converter could therefore better be motivated and may cover the total clean steam needs for the pre steaming and steaming system. More of the steam from the steam net of the mill i.e. that produced conventionally in the recovery boiler dome, could be used for energy production in steam driven generators producing environmental friendly electricity from recovery operations that classifies as green electricity as it is produced from energy recovery.