WO2021129926A1 - Appareil de production d'une poudre cristalline d'un matériau - Google Patents

Appareil de production d'une poudre cristalline d'un matériau Download PDF

Info

Publication number
WO2021129926A1
WO2021129926A1 PCT/EP2019/086949 EP2019086949W WO2021129926A1 WO 2021129926 A1 WO2021129926 A1 WO 2021129926A1 EP 2019086949 W EP2019086949 W EP 2019086949W WO 2021129926 A1 WO2021129926 A1 WO 2021129926A1
Authority
WO
WIPO (PCT)
Prior art keywords
heat
heat exchanger
hot
dryer
air
Prior art date
Application number
PCT/EP2019/086949
Other languages
English (en)
Inventor
Carsten Juhl JESSEN
Thibault LEGRAND-LOPES
Original Assignee
Gea Process Engineering A/S
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 Gea Process Engineering A/S filed Critical Gea Process Engineering A/S
Priority to PCT/EP2019/086949 priority Critical patent/WO2021129926A1/fr
Publication of WO2021129926A1 publication Critical patent/WO2021129926A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/16—Evaporating by spraying
    • B01D1/18—Evaporating by spraying to obtain dry solids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/10—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it
    • F26B3/12—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it in the form of a spray, i.e. sprayed or dispersed emulsions or suspensions
    • 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 present invention relates to an apparatus for providing a crystal line powder of a material, comprising: an evaporator for warming and concen trating a liquid solution of said material, said evaporator being adapted to be energized by an external power source; a crystallizer for cooling the concen trated liquid solution for the material to crystalize; and a dryer for drying crys tallized material, with a hot air inlet for subjecting the crystallized material to hot air to provide a dried crystalline powder.
  • An apparatus of the above kind is as such known in the art and is used e.g. for producing lactose powder.
  • drying is a mass transfer process consisting of the removal of a solvent, the solvent being e.g. water and/or organic liquids as explained in the opening part of WO 2018/091049 A1 , incorporated herein by reference, and whereas the present invention is not limited to a specific solvent, water is used herein as a general example.
  • a solvent e.g. water and/or organic liquids as explained in the opening part of WO 2018/091049 A1 , incorporated herein by reference, and whereas the present invention is not limited to a specific solvent, water is used herein as a general example.
  • air is referred to herein as the medium used in the dryer for drying the crystalline material
  • another suitable gas than atmospheric air could be used and the term “air” as used herein is intended to include such gas.
  • the dryer a number of different kinds of apparatuses may be used such as e.g. spray dryers, flash dryers, ring dryers, fluidized bed dryers, belt dryers, etc.
  • the process disclosed in WO 2018/091049 A1 relates to drying whereby at least a base amount of heat for heating air to be let into the dryer for subjecting a material to be dried to hot air, is provided by a heat pump.
  • a dew point dehu midification is used together with latent and/or sensible heat from exhaust gas from the dryer, whereby a varying potential of heat from the dew point dehu midification is compensated by an appropriate amount of the latent and/or sen sible heat of the exhaust gas to provide a source for meeting a substantially constant demand of energy for the heating of air to be let into the dryer.
  • an apparatus as mentioned by way of introduction further comprises: a heat pump adapted to transfer heat energy from a cold side to a hot side by means of a first circuit circulating a refrigerant, the hot side comprising a hot part and a very hot part, the heat pump comprising first heat exchangers, the first heat exchangers comprising: a cold heat exchanger at tached to the cold side; a hot heat exchanger attached to the hot part; and a very hot heat exchanger attached to the very hot part, said first heat exchang ers forming part of the first circuit and being adapted to exchange heat energy with a second circuit comprising several physically interconnected loops and being adapted to circulate a heat transfer fluid between said first heat exchang ers and peripheral heat exchangers, the peripheral heat exchangers comprising: a crystallization heat exchanger provided in a loop connected to the cold heat exchanger and adapted to provide for cooling the concentrated liquid so lution in the crystallizer; a pre-heat heat exchanger provided in a
  • crystallizer heat exchange may e.g. be performed either via a heat exchanger (external) or directly on a jacket of crystallization tanks by cir culating the heat transfer fluid of the second circuit through said jacket(s).
  • Using a heat pump to provide for cooling of the crystallizer entails that the need for using ice-water in the process, as is known, may be avoided.
  • the second circuit will in operation be circulating a fluid heat transfer medium, i.e. a heat transfer fluid, e.g. water.
  • a fluid heat transfer medium i.e. a heat transfer fluid
  • water e.g. water
  • the fluid heat transfer me dium circulated in the second circuit will herein i.a. be referred to as water though it should be understood that any other suitable fluid medium may be used within the scope of the present invention.
  • Water emerging from the cold heat exchanger may have a tempera ture in a range from 0.5 - 4°C and up to 8 - 12°C
  • water emerging from the hot heat exchange may have a temperature in the range of 30°C to 75°C
  • water emerging from the very hot heat exchanger may have a temperature in the range of 75°C to 135°C or 140°C or more, according to the potential of the heat pump.
  • heat pump as an example a heat pump using CO2 as a medium and operating a cycle at least partially in supercritical condition may be used in con nection with the present invention.
  • the apparatus preferably comprises a control device for controlling the operation of the heat pump and the second circuit.
  • the apparatus may include any such valves, pumps, sensors, etc. that the skilled person will appreciate.
  • the second circuit is typically configured to be controlled by flow, flow direction, pressure and temperature in respective parts of said second circuit to manage transfer of heat from each of the con dense heat exchanger and the crystallization heat exchanger to the heat trans fer fluid, from the heat transfer fluid to the cold (evaporation) side of the heat pump, from any hot side of the heat pump to the heat transfer fluid, and from the heat transfer fluid to each of the pre-heat heat exchanger and the main- heat heat exchanger.
  • the dryer is a spray dryer and comprises an atom izer for atomizing a liquid solution comprising the crystalized material and the spray dryer is configured for subjecting the atomized liquid solution to the hot air to provide a dried crystalline powder.
  • the atomizer may be any kind of at omizer known in the art, e.g. a rotary atomizer or a nozzle, e.g. a pressure nozzle or a two-fluid nozzle, etc.
  • the dryer may be e.g. a fluid bed dryer or a flash dryer, etc.
  • a source of steam is attached to the evaporator to provide energy for warming the liquid solution in the evaporator.
  • a solvent heat exchanger provided in a loop con nected to the cold heat exchanger is attached to the evaporator and adapted to provide for cooling solvent removed from the liquid solution.
  • solvent removed from the liquid solution In a known ap paratus such removed solvent is cooled using ice-water. In this embodiment of the present invention use of ice-water is further avoided.
  • an exhaust air heat exchanger is provided in a loop connected to the cold heat exchanger and adapted to exchange heat energy with air exhausted from the dryer.
  • a secondary dryer downstream of an outlet for crystalline powder from the dryer, a secondary dryer is provided downstream of an outlet for crystalline powder from the dryer.
  • a secondary hot air inlet is provided for letting in secondary hot air into the secondary dryer.
  • the apparatus may comprise at least one of a secondary pre-heat heat exchanger provided in a loop con nected to the hot heat exchanger and adapted to heat air for the secondary dryer upstream of the inlet; and a secondary main-heat heat exchanger pro vided in a loop connected to the very hot heat exchanger and adapted to heat air for the hot air inlet of the secondary dryer upstream of the inlet.
  • a cool air inlet may be provided for letting in cool air into the secondary dryer.
  • a desiccant device may be provided upstream of the cool air inlet for desiccating the cool air to be let into the secondary dryer.
  • the secondary dryer may e.g. be a fluid bed dryer with a vibrating bot tom plate that provides for transportation of the crystalline powder being dried in the secondary dryer in a generally horizontal direction, preferably from a sec tion comprising the secondary hot air inlet, through a section comprising the cool air inlet, and to an outlet for the dried crystalline powder.
  • Herby is obtained the possibility of initially drying residual moisture from the powder emerging from the first dryer by means of hot air and subsequently further drying and cooling the powder by means of cool dry air before letting out the powder prod uct.
  • the desiccant device is a desiccant wheel and a cool air heat exchanger is provided in a loop connected to the cold heat ex changer and adapted to exchange heat energy with air between the desiccant wheel and the cool air inlet.
  • a regeneration air inlet is provided for letting in regeneration air into the desiccating wheel for regen erating the same, and a regeneration air heat exchanger is provided in a loop connected to one of the hot heat exchanger and the very hot heat exchanger and adapted to heat regeneration air upstream of the regeneration air inlet.
  • a connection is provided, e.g. through a sec ond external heat exchanger, to an external source to provide additional heat ing to the regeneration air upstream of the inlet of the desiccant wheel.
  • the temperature of the regeneration air may be raised to a higher level than provided for by the heat pump.
  • an apparatus for providing a crystalline powder of a material comprises: an evaporator 10 for warming and concentrating a liquid solution of said material, said evaporator being adapted to be energized by an external power source, such as a source of steam 11 ; a crystallizer 20 for cool ing the concentrated liquid solution for the material to crystalize; and a dryer 30 for drying crystallized material, with a hot air inlet 31 for subjecting the crystal lized material to hot air to provide a dried crystalline powder.
  • an external power source such as a source of steam 11
  • a crystallizer 20 for cool ing the concentrated liquid solution for the material to crystalize
  • a dryer 30 for drying crystallized material, with a hot air inlet 31 for subjecting the crystal lized material to hot air to provide a dried crystalline powder.
  • the evaporator 10 receives in operation a liquid solution of the material to be crystallizes. From the evaporator 10 liquid solvent removed from the liquid solution is let out at an outlet 12 as a hot or warm liquid of e.g. 20-25°C. In a known process, depending on the further use or disposal of the warm liquid, this warm liquid may be cooled to e.g. 8-12°C using ice-water.
  • the external power source or source of energy for the evapo rator 10 may be electric and the heating of the liquid solution in the evaporator 10 may be obtained e.g. by the technic known in the art as Mechanical Vapour Recompression.
  • the apparatus further com prises: a heat pump 40 adapted to transfer heat energy from a cold side to a hot side by means of a first circuit circulating a refrigerant, the hot side com prising a hot part and a very hot part, the heat pump comprising first heat ex changers.
  • the first heat exchangers comprise: a cold heat exchanger 41 at tached to the cold side; a hot heat exchanger 42 attached to the hot part; and a very hot heat exchanger 43 attached to the very hot part, said first heat ex changers 41 , 42, 43 forming part of the first circuit.
  • the first heat exchangers 41 , 42, 43 are adapted to exchange heat energy with a second circuit 50 com prising several physically interconnected loops and being adapted to circulate a heat transfer fluid between said first heat exchangers and peripheral heat exchangers.
  • the peripheral heat exchangers comprise: a condense heat exchanger 55 provided in a loop connected to the cold heat exchanger 41 and adapted to exchange heat energy with evaporated solvent, e.g. water, from the evaporator 10 and possible surplus steam from the ener gizing, whether the energizing is obtained by steam through the source of steam 11 or by Mechanical Vapour Recompression; a solvent heat exchanger 51 provided in a loop connected to the cold heat exchanger 41 and adapted to exchange heat energy with the hot or warm liquid solvent, e.g.
  • evaporated solvent e.g. water
  • a crystallization heat exchanger 52 provided in a loop connected to the cold heat exchanger 41 and adapted to provide for cooling the concentrated liquid solution in the crystallizer 20; a pre-heat heat exchanger 53 provided in a loop connected to the hot heat exchanger 42 and adapted to heat air for the hot air inlet 31 of the dryer 30 upstream of the hot air inlet 31 ; and a main-heat heat exchanger 54 provided in a loop connected to the very hot heat exchanger 43 and adapted to heat air for the hot air inlet 31 of the dryer 30 upstream of the hot air inlet 31 and downstream of the pre-heat heat exchanger 53.
  • the solvent heat exchanger 51 is optional since cooling of the outlet liquid solvent may not be needed. In a known process cooling of the outlet liquid solvent is performed by means of ice-water. Thus, using in accordance with the present invention the solvent heat exchanger 51 a need for ice-water in the process may be avoided.
  • the apparatus also comprises an additional loop of the second circuit 50 that is provided for connecting the hot heat ex changer 42 or the very hot heat exchanger 43 with an external heat sink 60.
  • the external heat sink 60 may e.g. be a hot water reservoir in a facility providing for cleaning-in-place of the apparatus and/or other apparatuses nearby, that are adapted for cleaning-in-place. It is noted that cleaning-in-place, commonly known as CIP, is as such a well-known technology.
  • the apparatus comprises a con nection, e.g. through a first external heat exchanger 71 , to an external source 70 to provide additional heating to the inlet air upstream of the hot air inlet 31 of the dryer 30.
  • a con nection e.g. through a first external heat exchanger 71
  • an external source 70 to provide additional heating to the inlet air upstream of the hot air inlet 31 of the dryer 30.
  • This may provide for heating, if needed, the air for the hot air inlet 31 to a temperature level not obtainable by means of the heat pump 40.
  • the heat pump 40 and second circuit 50 together may be configured to at least fulfil the cooling needs of the crystallizer 20 and possibly also of the evaporator 10.
  • the embodiment shown comprise a control device 80 for controlling the operation of the heat pump 40 and the second circuit 50.
  • the second circuit is configured to be controlled by flow, flow direction, pressure and tem perature in respective parts of said second circuit to manage transfer of heat from each of the condense heat exchanger and the crystallization heat ex changer to the heat transfer fluid, from the heat transfer fluid to the cold (evap oration) side of the heat pump, from any hot side of the heat pump to the heat transfer fluid, and from the heat transfer fluid to each of the pre-heat heat ex changer and the main-heat heat exchanger.
  • an exhaust air heat exchanger 56 is pro vided in a loop connected to the cold heat exchanger 41 and adapted to ex change heat energy with air exhausted from the dryer 30.
  • a secondary dryer 32 downstream of an outlet for crys talline powder from the dryer 30, a secondary dryer 32 is provided downstream of an outlet for crys talline powder from the dryer 30, a secondary dryer 32 is provided downstream of an outlet for crys talline powder from the dryer 30, a secondary dryer 32 is provided downstream of A secondary hot air inlet 33 may as shown be provided for letting in secondary hot air into the secondary dryer 32.
  • a secondary pre-heat heat exchanger 57 provided in a loop connected to the hot heat exchanger and adapted to heat air for the secondary dryer upstream of the inlet 33
  • a secondary main-heat heat exchanger 58 provided in a loop connected to the very hot heat exchanger and adapted to heat air for the hot air inlet of the secondary dryer 32 upstream of the inlet 33 may be provided or only one of these two heat exchangers 57. 58 may be provided.
  • a cool air inlet 34 may be provided for letting in cool air into the secondary dryer 32.
  • a desiccant device 90 may be provided up stream of the cool air inlet 34 for desiccating the cool air to be let into the sec ondary dryer 32.
  • the desiccant device may be a desiccant wheel 90 and a cool air heat exchanger 59 may be provided in a loop connected to the cold heat exchanger and adapted to exchange heat energy with air between the desic cant wheel 90 and the cool air inlet 34.
  • a regeneration air inlet 91 is provided for letting in regeneration air into the desiccating wheel for regenerating the same, and a regeneration air heat exchanger 92 is pro vided in a loop which in the present embodiment is connected to the hot heat exchanger 42 and adapted to heat regeneration air upstream of the regenera tion air inlet 91 .
  • connection is provided, e.g. as shown through a second external heat exchanger 93, to an external source 94 to provide additional heating to the regeneration air upstream of the inlet 91 of the desiccant wheel 90.
  • the apparatus described above may e.g. be used for producing lac tose powder (or a crystallized whey powder or derivative, such as whey per meate powder).
  • lac tose powder or a crystallized whey powder or derivative, such as whey per meate powder.
  • the evaporator 10 uses steam and/or electricity as energy (source 11 ) to remove water from the lactose. Residual steam from the energization, whether by a source of steam 11 or e.g. by mechanical vapour recompression, needs to be condensed which takes place in the condense heat exchanger 55, whereby a low pressure is maintained in the evaporator 10 to promote the evaporation of water and thus of concentration of the lactose.
  • lactose is transferred to the crystallizer 20 to be cooled down for several hours in order to create lactose crystals.
  • the crystallizer 20 may comprise several separate tanks. The cooling is provided for by cold water from the cold heat exchanger 41 of the heat pump through the crystallization heat exchanger 52.
  • Lactose crystals are subsequently sent to the dryer 30 where they are dried into lactose powder by removing the water part in it.
  • a spray dryer is used as the dryer 30, lactose crystals are sprayed into a hot and dry air stream in the dryer 30.
  • the air stream in the dryer may need to be hotter than the temperature provided for by the very hot heat exchanger 43 and thus the wanted or needed temperature may be obtained through external source 70 and the first external heat exchanger 71 .
  • a fluid bed dryer or a flash dryer is used the temperature of the hot and dry air provided by the very hot heat exchanger 43 may suffice. It is possible to include in an apparatus according to the invention a step of mechanical separation of the crystals produced in the crystallizer 20 before the drying step.
  • Such mechanical separation may e.g. be used before drying by means of a fluid bed dryer or a flash dryer.
  • Post drying air streams may be provided e.g. in the secondary dryer 32 through the sec ondary hot air inlet 33 and the cool air inlet 34 to provide the final product in a dry and cool condition as may be needed by the circumstances.
  • lactose e.g. whey powder
  • demineralized whey powder or whey permeate powder may be produced using an apparatus according to the present invention.

Landscapes

  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Sustainable Development (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Microbiology (AREA)
  • Drying Of Solid Materials (AREA)

Abstract

L'invention concerne un appareil de production d'une poudre cristalline d'un matériau, comprenant : un évaporateur (10) ; un cristalliseur (20) ; et un séchoir (30), et comprenant en outre : une pompe à chaleur (40) comportant : un échangeur de chaleur froide (41) ; un échangeur de chaleur chaude (42) ; et un échangeur de chaleur très chaude (43) qui est apte à échanger de l'énergie thermique avec un second circuit (50) comprenant : un échangeur de chaleur à condensation (55) relié à l'échangeur de chaleur froide (41) et à l'évaporateur (10) ; un échangeur de chaleur de cristallisation (52) relié à l'échangeur de chaleur froide (41) et au cristalliseur (20) ; un pré-échangeur de chaleur et un échangeur principal de chaleur (53, 54) reliés aux échangeurs de chaleur chaude et très chaude (42, 43) et à une entrée d'air chaud (31) du séchoir (30), cet appareil comprenant un dissipateur thermique externe supplémentaire (60) et/ou un échangeur de chaleur à solvant (51) et/ou une source externe (70) pour fournir un chauffage supplémentaire à l'air d'entrée en amont de l'entrée d'air chaud (31) du séchoir (30), et ainsi la pompe à chaleur (40) et le second circuit (50) sont conçus pour satisfaire les besoins de refroidissement du cristalliseur (20).
PCT/EP2019/086949 2019-12-23 2019-12-23 Appareil de production d'une poudre cristalline d'un matériau WO2021129926A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2019/086949 WO2021129926A1 (fr) 2019-12-23 2019-12-23 Appareil de production d'une poudre cristalline d'un matériau

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2019/086949 WO2021129926A1 (fr) 2019-12-23 2019-12-23 Appareil de production d'une poudre cristalline d'un matériau

Publications (1)

Publication Number Publication Date
WO2021129926A1 true WO2021129926A1 (fr) 2021-07-01

Family

ID=69165333

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2019/086949 WO2021129926A1 (fr) 2019-12-23 2019-12-23 Appareil de production d'une poudre cristalline d'un matériau

Country Status (1)

Country Link
WO (1) WO2021129926A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023083423A1 (fr) * 2021-11-12 2023-05-19 Gea Process Engineering A/S Système de chauffage reposant sur une pompe à chaleur efficace à récupération de chaleur
SE2251074A1 (en) * 2022-09-15 2024-03-16 Munters Netherlands B V A spray dryer arrangement and a method of controlling such an arrangement

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1187534A1 (fr) * 1999-05-31 2002-03-20 Apv Anhydro A/S Concentration de liquides
US20030196957A1 (en) * 2002-04-17 2003-10-23 Niro A/S Process and plant for evaporative concentration and crystallization of a viscous lactose-containing aqueous liquid
CN206549190U (zh) * 2016-12-27 2017-10-13 中山市中环环保废液回收有限公司 一种低温蒸发设备
WO2018091049A1 (fr) 2016-11-18 2018-05-24 Gea Process Engineering A/S Système de séchage à efficacité énergétique et commande de capacité améliorées
AU2016370303A1 (en) * 2015-12-15 2018-07-26 A. Kent Keller Dryer for lactose and high lactose products
CN207886733U (zh) * 2018-01-18 2018-09-21 广东慧源环境工程有限公司 一种浓水热泵结晶干燥装置

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1187534A1 (fr) * 1999-05-31 2002-03-20 Apv Anhydro A/S Concentration de liquides
US20030196957A1 (en) * 2002-04-17 2003-10-23 Niro A/S Process and plant for evaporative concentration and crystallization of a viscous lactose-containing aqueous liquid
AU2016370303A1 (en) * 2015-12-15 2018-07-26 A. Kent Keller Dryer for lactose and high lactose products
WO2018091049A1 (fr) 2016-11-18 2018-05-24 Gea Process Engineering A/S Système de séchage à efficacité énergétique et commande de capacité améliorées
CN206549190U (zh) * 2016-12-27 2017-10-13 中山市中环环保废液回收有限公司 一种低温蒸发设备
CN207886733U (zh) * 2018-01-18 2018-09-21 广东慧源环境工程有限公司 一种浓水热泵结晶干燥装置

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023083423A1 (fr) * 2021-11-12 2023-05-19 Gea Process Engineering A/S Système de chauffage reposant sur une pompe à chaleur efficace à récupération de chaleur
SE2251074A1 (en) * 2022-09-15 2024-03-16 Munters Netherlands B V A spray dryer arrangement and a method of controlling such an arrangement

Similar Documents

Publication Publication Date Title
WO2021129926A1 (fr) Appareil de production d'une poudre cristalline d'un matériau
US11085696B2 (en) Drying system with improved energy efficiency and capacity control
US10294122B2 (en) Seawater desalination device and seawater desalination method
CN105819531B (zh) 一种节能热泵型中温喷雾蒸发系统
JP2020500690A (ja) 低重力場により強化される多段蒸発システム
CN103209928B (zh) 水处理系统和水处理方法
CA3030589C (fr) Installation de distillation a basse temperature
KR970006989B1 (ko) 폐액, 특히 높은 고체함유량을 갖는 산업폐수를 처리하는 방법 및 장치
JPH07508207A (ja) 板形熱交換器による海水脱塩の方法及び装置
CN110746022B (zh) 污水处理系统
SE460869B (sv) Vaermepump av absorptionstyp
US4864830A (en) Air conditioning process and apparatus
JPS61500506A (ja) ヒ−トポンプの熱源として水の凍結熱を利用する方法および装置
JPH0952083A (ja) 海水淡水化装置
DK201670923A1 (en) Drying system with improved energy efficiency and capacity control
WO2023083423A1 (fr) Système de chauffage reposant sur une pompe à chaleur efficace à récupération de chaleur
EP4141222A1 (fr) Système d'énergie comprenant un sous-système de compression mécanique de la vapeur (cmv/rmv) et procédé de conversion d'énergie
CN1119950C (zh) 浓缩果汁或加工含有固体成分的水溶液的方法及设备
KR102315936B1 (ko) 하이브리드 수처리 장치 및 방법
WO2014196611A1 (fr) Dispositif de concentration et procédé de concentration
Atkins et al. Integration potential of milk powder plants using conventional heat recovery options
JP2017203558A (ja) 濃縮乾燥装置及び濃縮乾燥方法
JPH04330903A (ja) 水溶性有機物を含む水溶液の蒸発濃縮方法
JP2787182B2 (ja) 一重二重吸収冷温水機
RU2022607C1 (ru) Установка для получения сухого продукта

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19836498

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 19836498

Country of ref document: EP

Kind code of ref document: A1