US3492198A - Heat and turpentine recovery from pulp digesters - Google Patents

Heat and turpentine recovery from pulp digesters Download PDF

Info

Publication number
US3492198A
US3492198A US433548A US3492198DA US3492198A US 3492198 A US3492198 A US 3492198A US 433548 A US433548 A US 433548A US 3492198D A US3492198D A US 3492198DA US 3492198 A US3492198 A US 3492198A
Authority
US
United States
Prior art keywords
condenser
blow
pressure
valve
pipe
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US433548A
Other languages
English (en)
Inventor
Curt F Rosenblad
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rosenblad Corp
Original Assignee
Rosenblad Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rosenblad Corp filed Critical Rosenblad Corp
Application granted granted Critical
Publication of US3492198A publication Critical patent/US3492198A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/06—Treatment of pulp gases; Recovery of the heat content of the gases; Treatment of gases arising from various sources in pulp and paper mills; Regeneration of gaseous SO2, e.g. arising from liquors containing sulfur compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the nal temperature of the digester is usually about 170 C. and the pressure is about 7 atmospheres.
  • Most of the turpentine is released during the rst period of the cook.
  • the pressure is reduced by gas relief from the top of the digester to a pressure of about 4 or 5 atmospheres, after which the contents of the digester are blown into a blow tank.
  • a smaller part of the recovery of turpentine is also released by the gas relief from full pressure down to the pressure when blowing begins.
  • the system is provided with means connected to the top of the digester which receives the relief gasses therefrom, removes pulp and black liquor from the gases, and condenses the gases.
  • a turpentine recovery system of such type is shown, for example, in the patent to Nyl quist, No. 2,996,423. With such systems, the rate of recovery of turpentine is much lower than it should be on a theoretical basis, and the turpentine recovered usually requires further purication, since it is contaminated to some extent by at least small amounts of pulp and black liquor.
  • Nyquist recommends that only after the turpentine vapors have been conventionally recovered, the relief gases and vapors be conducted to the blow line and further to the jet condenser. In accordance with the method of Nyquist, therefore, turpentine vapors prevalent in that part of the relief, wrich is conducted to the blow line, are irretrievably lost.
  • the ow of coolinq liquid to the direct contact condenser is so controlled in relation to the flow of blow steam therethrough that some of the blow steam passes as such, that is, in condensed form, through the direct contact condenser.
  • the mixture of cooling liquid and condensate discharged from such condenser is maintained at or close to the boiling point.
  • a valve which automatically controls the ilow of cooling liquid into the direct contact condenser, and pressure responsive means disposed in the closed system either before or after the direct contact condenser for controlling such valve.
  • some of the blow steam is allowed to pass uncondensed through the jet condenser, whereby coolant passing from the jet condenser mixed with blow steam condensate will be kept at or even slightly above the boiling point and whereby the uncondensed portion of the blow steam will be condensed in the turpentine condenser, which iS connected with the jet condenser in series on the steam side and in which remaining heat will be recovered as Well as turpentine contained in said steam.
  • This over-pressure can be held at some four to twelve inches of water column up to p.s.i.g. at the beginning and prevalence of the blow to be dissipated down to close to atmospheric pressure at the end of the blow, an overpressure completely without harmful effects for the smooth completion of the blow.
  • a further object of the invention is to provide an improved method of blow steam recovery which is characterized by the improvement in the amount of turpentine recovered from the system and the purity of the thus recovered turpentine.
  • Another object of the invention is to provide an improved method of blow steam recovery in systems of the type described wherein the condensate in the upper layers of the accumulator is maintained at or substantially at the boiling point and wherein there is less contamination of the condensate in the accumulator.
  • Still another object of the invention is to provide an improved blow steam recovery system for carrying out the method of the invention.
  • FIG. 1 is a diagrammaic illustration of a rst embodiment of a heat recovery system in accordance with the invention and for carrying out the method thereof;
  • FIG. 2 is a composite graph of a single blow of a digester discharge cycle, said figure showing the regular flow of steam in pounds per minute and the blow pressure, both such values being plotted against blowing time in minutes;
  • FIG. 3 is a diagrammatic illustration of a second embodiment of a heat recovery system in accordance with the invention and for carrying out the method thereof.
  • FIG. 1 a single digester for the cooking of pulp is illustrated at 1, said digester being discharged through a suitable header to a common single blow tank, as shown here at 2.
  • the digester 1 will be referred to, it is, of course, to be understood when not otherwise specified that the digester 1 could be any one in the bank, whether the number employed is four or otherwise.
  • the digester 1 has an opening neck 5 suitably closed by a cover 6.
  • a gas relief pipe 7 extends from one side of the digester neck 5 and is in communication with the interior of the digester so that gases collecting in the upper portion thereof can be relieved through that pipe.
  • a relief valve 8 in the pipe 7 controls the ow through that pipe and from the valve 8 the pipe continues into communication with the common gas relief header 9 for all of the digesters in the bank.
  • This header normally continues past a normally open valve (not shown) into communication with the interior of the blow tank 2 adjacent its top 12.
  • the top 12 of the blow tank is provided with a safety outlet pipe 16 provided with a safety pressure release damper 17.
  • An outlet or blow pipe 20 is connected to the top 12 of blow tank 2 as shown at 21, such pipe 20, in the illustrative embodiment, extending directly into the top, vaporcontaining space 33 of an accumulator tank 23, to be described.
  • a direct condenser 22 mounted upon the top of the accmulator tank 23 and directly communicating with the vapor-containing space 33 in the tank is a direct condenser 22.
  • the direct condenser 22 may be of various types, but as here illustrated, and as explained in the foregoing, it is generally of the type detailed in my co-pending application Ser. No. 220,386, above referred to.
  • bafe and direction changing means as shown at 27, 28, 29, 30, and 31.
  • bafe and direction changing means as shown at 27, 28, 29, 30, and 31.
  • the accumulator tank 23 has a rounded upper end 32 which usually provides the gas chamber or vaporcontaining space 33 therein. Below that the tank is cylindrical, as shown at 34.
  • the accumulator tank 23 provides the reservoir for hot and cooled liquid, hot in the upper portion of the tank and cooled in the lower portion achieved by a re-circulating system, to be described.
  • That re-circulating system for the contents of the accumulator tank consists of a withdrawing element 35 within the tank close to the upper portion of the cylindrical wayy thereof, element 35 being connected to the pipe 36 through which hot condensate from the top of the tank 23 is drawn off.
  • the pipe 36 is connected to a discharge pump 39 which forwards hot condensate under pressure through a pipe 40.
  • Such pipe 40 may, if desired, be connected to an indirect heat exchanger (not shown) for the heating of process water, for example.
  • the heat recovery system illustrated herein includes an after-condenser or indirect heat exchanger 56 which has sufficient capacity to take care of all the blow steam vapors, and non-condensable gases which are discharged through blow pipe 20 during the second portion of the discharge cycle.
  • the turpentine formed from the condensing of its gases in such mixture runs off through the pipe 57 from the after-condenser while the remaining non-condensable portion of such gas mixture can be vented to atmosphere or otherwise disposed of through a vent pipe 58.
  • the after-condenser 56 is provided with an ample supply of cooling water through a pipe connected to port 59 of the after-condenser. Cooling water which is discharged from the after-condenser 56 flows therefrom through a pipe 47 which may either enter the bottom of the accumulator tank 23, as shown, or lead to a discharge sump.
  • the after-condenser 56 in the first portion of the blow or discharge cycle of the vessel or digester 1, is fed with vapors and non-condensable gases from the vapor-containing space of the accumulator and/or t-he direct condenser 22, being then disconnected from direct connection to the blow pipe 20,
  • the after-condenser 56 is shut off from direct communication with the vapor-containing space of the accumulator 23 and/or the direct condenser 22 and is then fed with the remaining blow steam, vapors, and non-condensable gases directly from the blow pipe 20.
  • these operations are effected automatically by the following mechanisms.
  • the end of the blow pipe 20, inwardly of the accumulator tank 23 at the position 89 at which the pipe enters the tank, is provided with a check valve 90 which remains open so long as the pressure of the blow steam in pipe exceeds said desired predetermined value and closes automatically when such pressure drops below such value.
  • a second, by-pass pipe or conduit 55 is connected between conduit 20 outwardly of valve 90 and the inlet port of the after-condenser 56.
  • a third conduit 62 is connected between conduit 55 and the direct condenser 22. It is to be understood, however, that conduit 62 may, if desired, be connected to the upper end 32 of the accumulator tank 23.
  • Interposed in conduit 55 between conduit 20 and conduit 62 is a selectively operated shut-olf valve 60.
  • Valve 61 Interposed in conduit 62 is a Valve 61 which may be selectively operated to place it in closed or open position. In said open position the valve 61 operates as a pressure-responsive relief valve to permit the passage of gases therethrough from the direct condenser 22 to the conduit 55 when such gases exceed the predetermined pressure relief value for which the valve 61 is set. Valve 61 may be set, for example, so that when it is in open position, it passes gases from condenser 22 at a pressure of 5 p.s.i.g. and above.
  • the accumulator tank 23 is also provided with a pressure relief conduit 70 rising from the vapor-containing space thereof, pipe 70 being provided with a pressure relief valve for damper 71.
  • the pressure relief valve 71 may be set to open, for example, at a pressure of 7 p.s.i.g.
  • the direct condenser 22 is provided with cooling liquid in the manner illustrated and claimed in the application of Axel E. Rosenblad, Ser. No. 374,208, filed June 10, 1964.
  • the pipe or conduit leading to the direct condenser 22 is fed from an intake device 84 lying adjacent the bottom of the accumulator tank 23, device 84 thus being positioned to withdraw the coolest condensate from the accumulator. Condensate entering the device 84 flows through a pipe 83 to the intake port of a force pump 82 of large capacity.
  • a pipe 85 Connected in shunt with the pump 82 and with the pipe 25 and the lower end of the space within the accumulator tank 23 is a pipe 85 which has a selectively operable shut-off valve 86 interposed therein.
  • the intake port 24 of condenser 22 is positioned substantially above the pump 82. When valve 86 is fully opened, it passes a sufficient portion of the output of pump 82 to maintain the level of condensate in the pipe 25 somewhat below the upper, generally horizontal run thereof.
  • the pump 82 When, however, the valve 86 is closed, the pump 82 immediately delivers its full output directly to the inlet port 24 of condenser 22-
  • the mechanism here shown is particularly advantageous because of the speed with which it responds selectively to deliver cooling fluid to the direct condenser 22 when required and to shut off the flow of such uid to such condenser.
  • the level of the liquid in the accumulator tank 23 is preferably maintained substantially constant as at the line 48.
  • the discharge valve 72 positioned adjacent the lower end of tank 23, when opened -by the float mechanism 73, discharges into a surge tank 74. Condensate from the surge tank 74 is withdrawn therefrom by a pump 77 and forwarded to a heat exchanger 75 which may be of the indirect type. Heated condensate enters heat exchanger 75 through the conduit 76 and is discharged therefrom through conduit 78. Cooled water enters the heat exchanger through a conduit 79 and is discharged as hot water through a conduit 80.
  • the system incorporates means whereby should the pressure within the vapor-containing space 33 of the accumulator tank fall below the desired predetermined value live steam is injected directly into such space.
  • Such means takes the form of a steam injecting pipe 87 connected to a source of live steam (not shown), a pressure controlled shut-off valve 88 being interposed in pipe 87.
  • Valve 88 which is of conventional design, is arranged to open and discharge live steam into space 33 whenever the pressure in such space falls below said desired predetermined value.
  • valve 60 is under the control of the check valve 90, as by means of an electrical contact on such valve interposed in a control circuit, schematically indicated at 66, connected to valve 60.
  • the pump 82 which introduces cooling fluid to the direct condenser 22, is also preferably automatically controlled.
  • an orifice 63 in conduit 55 between the location of connection of the conduit 62 thereto and the entrance port of the after-condenser 56.
  • Such orifice which detects the lrate of flow of gases therethrough and thus pressure differences on the two sides thereof, is connected by a control circuit 67 to a differential cell 68 which in turn is connected through a control circuit 69 to the operating means for the lby-pass valve 86.
  • Valve 86 is provided with a conventional control means, not specifically shown, whereby such valve is held in open position during the end of the first portion of the discharge cycle, when valve 90 is closed and valve 60 is opened. As a result, at such time the flow of cool condensate into the direct contact condenser 22 is avoided.
  • the described system of FIG. l operates as follows: Before the start of a blow or discharge cycle, the whole system, including the blow tank 2, is under a slight pressure, of, for example, l0 inches of water column. When the digester valve 4 opens and the blow starts, the pressure in the digester drops very rapidly, as is shown in the pressure-time graph of FIG. 2. The blow pressure drops, for example, from to 6 p.s.i.g in 61/2 minutes. During this time, which is termed the first portion of the discharge cycle, the valve 90 in blow pipe 20 is open. Valve 61 may open partly or fully in functioning as a pressure relief to keep the pressure in the accumulator and the condenser 22 at a predetermined value, for example 6 p.s.1.g.
  • the pressure control valve 90 shuts automatically, as does the check valve 61. Simultaneously with the closing of valve 90 the valve 60 opens, thereby yby-passing the remainder of the blow steam during the second portion of the discharge cycle. Accordingly, the space 33 within the accumulator 23 and Within the direct condenser 22 is shut off from the blow tank.
  • the blow steam including vapors and noncondensable gases, then passes through the orifice 63 directly to the after-condenser 56.
  • the differential cells 68 opens the by-pass valve 86 of the cooling fluid delivery system, thereby stopping the delievery of cooling condensate to the condenser 22.
  • valve 60 automatically closes and valve 61 assumes its open position at which it functions as a pressure relief valve. The system is now ready for a fresh blow or discharge cycle.
  • the average temperature of hot condensate at the top of the accumulator is 200 F.
  • hot condensate can be produced and maintained in the upper portion of the accumulator at a temperature of 230 F. when the accumulator is held at a pressure of 6 p.s.i.g. pressure.
  • the higher temperature of hot condensate in the accumulator makes possible the above noted marked economies in the heating surface of heat exchangers utilizing the hot condensate as a source of heat, in the accumulator volume requirement, and in the requirements for pumps, pipes, and conduits for supplying cooled condensate.
  • the maintenance of the hot condensate continuously under substantially constant pressure in the accumulator makes possible the continuous discharge of hot condensate of substantially constant temperature. This is accomplished with the transfer of the vapors, released during the pressure drop from 6 p.s.i.. down to atmospheric pressure, directly to the after condenser.
  • This after condenser should have ample size for preheating fresh Water to a temperature which is satisfactory for such water to be used as process water.
  • the after condenser should also have sufficient heating surface to sub-cool the turpentine condensate mixture.
  • the quantity of heat collected in the accumulator will be correspondingly reduced, but the temperature of the hot condensate in the described system will have a higher than conventional temperature level, varying between 230 and 212 F.
  • FIG. 3 there is shown a conduit 10, to which other digesters, not shown, which are not connected to the condenser 11, are connected.
  • the header, here designated 9 for the digester 1 shown is connected to the header 10 so that both discharge into the upper end of the blow tank 2 through the relief conduit 9.
  • the upper end of the blow tank is connected by a blow Iconduit 10 to the direct contact condenser-accumulator combination.
  • the discharge end of the conduit 10 is connected to the upper end of the condenser 11. It is immaterial whether the condensate flows in countercurrent to the cooling liquid, as in FIG l, or in the same direction as the cooling liquid, as in FIG. 3.
  • the accumulator 13 of FIG. 3 is shown as being provided with an overflow pipe 49 which extends from near the bottom of the tank to an inverted U-shaped portion at the desired top of the surface of the condensate in the tank, the overow pipe "being connected outwardly of the tank to a conventional trap 50. As a result, the level of condensate within the accumulator tank is maintained su-bstantially at the line 48.
  • the vapor space within the upper end of the accumulator tank 13 is connected at all times by the pipe 55 to the gas inlet end of the gas cooler 56.
  • gas cooler which is preferably of spirally wound construction, is so made and operated that it maintains its gas-connected indirectly cooled surfaces sufficiently cool to condense turpentine thereon.
  • an orifice-providing diaphragm 63 Interposed in the pipe 55, through which gas is fed to the gas coolerl 56, is an orifice-providing diaphragm 63 which operates a differential pressure sensing device 52 in the control circuit 67, such circuit extending to a flow responsive control 51.
  • the diaphragm 63 also functions to throttle the flow of vapor into the gas cooler 56 to create a desirable back pressure on the vapor
  • diaphragm 63 may be disposed in the outlet pipe 94 from the gas cooler, where it would also function as a differential pressure sensing and vapor throttling device.
  • Such portion of the system of FIG. 3 operates in the same manner as that of FIG. 1.
  • control system 63, 52, 67, 5S, 69, 86 operates to discharge cooling water into the upper end of the direct contact condenser 11, the flow responsive control 51 causing cooling water to flow in proportion to the discharge of blow steam into the condenser.
  • the ow of cooling water thereto is stopped.
  • the gas cooler 56 is fed with cooling water through a pipe 81 which has a temperature responsive valve 91 interposed therein.
  • Valve 91 is under the control of ternperature responsive means, not shown, whereby the temperature of the water discharged from the cooler through the pipe 92 for use, for example, in the mill, is maintained constant.
  • Uncondensed gases discharged from the gas cooler 56 pass to a vent through a pipe 96, condensed vapor from such gases being discharged from the cooler through a pipe 93.
  • Condensed turpentine is discharged from the cooler 56 through a pipe 94 which leads to a sub-cooler which is generally designated 95.
  • the sub-cooler may be either of the air or water cooled type, here being shown to be of the latter type and as being supplied with coolingr Water through a pipe 97, the cooling water being discharged through a pipe 98.
  • the resulting cooled turpentine flows downwardly through a discharge pipe 99 and into a decanter 100 from which it may 'be withdrawn through outlets 101, 102, and 103 disposed at progressively higher levels.
  • a vertically disposed sight glass 104 is provided on the decanter as shown. Any water which flows into the decanter settles at the lower end thereof so that it may be withdrawn through a water outlet conduit 105 provided with a manually operated discharge valve 106.
  • the gas cooler 56 is so constructed and arranged and is so operated as to condense turpentine from the vapors passing therethrough.
  • the principal constituent of oil of turpentine is pinene, CwHls, which boils at 156 C.
  • the vaporcontacting surfaces of the gas cooler 56 are thus maintained cool enough to condense the condensible components in the vapor flowing into the gas cooler, that is, at a temperature somewhat below 156 C.

Landscapes

  • Paper (AREA)
  • Cookers (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
US433548A 1964-09-29 1965-02-18 Heat and turpentine recovery from pulp digesters Expired - Lifetime US3492198A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US40016864A 1964-09-29 1964-09-29
US43354865A 1965-02-18 1965-02-18

Publications (1)

Publication Number Publication Date
US3492198A true US3492198A (en) 1970-01-27

Family

ID=27016931

Family Applications (1)

Application Number Title Priority Date Filing Date
US433548A Expired - Lifetime US3492198A (en) 1964-09-29 1965-02-18 Heat and turpentine recovery from pulp digesters

Country Status (5)

Country Link
US (1) US3492198A (fi)
AT (1) AT260675B (fi)
DE (1) DE1517214A1 (fi)
FI (1) FI46535C (fi)
NO (1) NO120868B (fi)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3607617A (en) * 1968-08-09 1971-09-21 Scm Corp Turpentine recovery from the wet gaseous effluent of wood-pulping processes
US4137134A (en) * 1976-04-20 1979-01-30 Oy W. Rosenlew Ab. Method for the recovery of sulphur compounds, volatile alcohols, turpentine and the like produced in connection with pulping
US4789428A (en) * 1985-07-11 1988-12-06 Ahlstromforetagen Svenska Ab Method for evaporation of spent liquor
US4915784A (en) * 1989-05-03 1990-04-10 Reynolds Ellis W Process and apparatus for removing contaminants from pulp digester vent gas
US9377240B2 (en) 2010-06-02 2016-06-28 Robert J Foxen System and method for recovering turpentine during wood material processing

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1469958A (en) * 1920-08-25 1923-10-09 Brown Co Apparatus for and method of recovering waste gases
US2803540A (en) * 1956-03-06 1957-08-20 Condi Engineering Corp Wood chip digestion
US2808234A (en) * 1953-05-27 1957-10-01 Rosenblads Patenter Ab Apparatus for condensing steam
US3286763A (en) * 1964-10-19 1966-11-22 Jacoby Process Equipment Co In Recovering heat from a blow evaporator for use in a surface evaporator
US3289736A (en) * 1964-06-30 1966-12-06 Rosenblad Corp Temperature control for evaporation system

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1469958A (en) * 1920-08-25 1923-10-09 Brown Co Apparatus for and method of recovering waste gases
US2808234A (en) * 1953-05-27 1957-10-01 Rosenblads Patenter Ab Apparatus for condensing steam
US2803540A (en) * 1956-03-06 1957-08-20 Condi Engineering Corp Wood chip digestion
US3289736A (en) * 1964-06-30 1966-12-06 Rosenblad Corp Temperature control for evaporation system
US3286763A (en) * 1964-10-19 1966-11-22 Jacoby Process Equipment Co In Recovering heat from a blow evaporator for use in a surface evaporator

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3607617A (en) * 1968-08-09 1971-09-21 Scm Corp Turpentine recovery from the wet gaseous effluent of wood-pulping processes
US4137134A (en) * 1976-04-20 1979-01-30 Oy W. Rosenlew Ab. Method for the recovery of sulphur compounds, volatile alcohols, turpentine and the like produced in connection with pulping
US4789428A (en) * 1985-07-11 1988-12-06 Ahlstromforetagen Svenska Ab Method for evaporation of spent liquor
US4915784A (en) * 1989-05-03 1990-04-10 Reynolds Ellis W Process and apparatus for removing contaminants from pulp digester vent gas
US9377240B2 (en) 2010-06-02 2016-06-28 Robert J Foxen System and method for recovering turpentine during wood material processing

Also Published As

Publication number Publication date
AT260675B (de) 1968-03-11
FI46535C (fi) 1973-04-10
DE1517214A1 (de) 1969-05-29
FI46535B (fi) 1973-01-02
NO120868B (fi) 1970-12-14

Similar Documents

Publication Publication Date Title
CA2565358C (en) Fiberline system and method using black liquor flashed steam
US3492198A (en) Heat and turpentine recovery from pulp digesters
US3063681A (en) Transfer of heat from superheated vapor in a condensing heat exchanger
WO2015124828A1 (en) Evaporator
CA1135100A (en) Method of cooking cellulose material
GB1111771A (en) Cooling system
CN101966396B (zh) 一种蒸发装置
US3362132A (en) Pressure responsive method for deaerating water
US2029360A (en) Heat recovery system
NO771330L (no) Fremgangsm}te ved cellulosekoking.
US5382321A (en) Process for the concentration of spent liquors
US2808234A (en) Apparatus for condensing steam
US2885328A (en) Sea water evaporating and distilling plant
US3745063A (en) Process for simultaneous turpentine recovery and odor control
US3286763A (en) Recovering heat from a blow evaporator for use in a surface evaporator
US838195A (en) Process of distillation.
US4686938A (en) System for heating liquid in a separator
US3155611A (en) Apparatus for treatment of sewage and like sludges
US6887345B2 (en) Process and device for evaporating liquids, for example black liquor from cellulose cooking, which contain solid and dissolved substances
US5944950A (en) Process for the final evaporation of black liquor
US3289736A (en) Temperature control for evaporation system
US2880146A (en) Apparatus for evaporating fluids
US2943124A (en) Hydrocarbon hydrate separation process and separation unit therefor
US1885561A (en) Accumulator system
US10815617B2 (en) Method for generation of clean steam in a continous digester system