ISO 13205:2024 海洋技術 — 海水淡水化 — 語彙 | ページ 6

3.1.1

海水淡水化

海水から生物や塩分などの余分な物質を除去し、市水や工業用水などとして利用できるようにする処理。

3.1.2

海水淡水化システム

海水淡水化 (3.1.1) プロセス用の相互に関連または相互作用するユニットのセット (原水 取水 (3.2.1) システム、 前処理 (3.3.1) 施設、膜および蒸留分離装置、後処理施設、および電子制御を含む)ユニットなど

3.1.3

源水

原水

海水淡水化システムに供給される入口水（3.1.2）

3.1.4

給水

海水淡水化システムの個々のコンポーネントまたは装置に供給される入口水 (3.1.2)

3.1.5

脱塩水

蒸留および膜脱塩プラントによって生成される淡水

3.1.6

製品水

鉱化（3.6.4） や 水の混合（3.6.5 ）などの 脱塩水（3.1.5） の 後処理（3.6.3） によって生成される水

3.1.7

塩水

海水よりも高い塩分濃度で、脱塩を行う膜または蒸留装置からの流れを濃縮（除去）すること。

3.1.8

集中係数

CF

濃縮液中の成分の濃度[濃縮液、 ブライン(3.1.7) ]と供給液中の全成分の濃度との比

注記 1:濃縮係数 (CF) は一般にC _b / C _f ここで, C _b は塩水濃度、 C _f は給水濃度です。

3.1.9

回収率

透過水量と供給量の比

[出典:ISO 23070:2020, 3.10]

3.1.10

要素

膜を含むコンポーネント。中空糸、らせん状カートリッジ、カセットなど、通常は交換可能

[出典:ASTM D6161-2019, 5.1, 修正 - 「中空糸」が定義に追加されました。]

3.1.11

モジュール

膜 エレメント (3.1.10) とエレメントのハウジングの組み合わせ

注記 1: 圧力容器 (3.4.3) には膜エレメントが含まれています。

[出典:ASTM D6161-2019, 5.1, 修正 — 元の定義の一部がエントリの注 1 に移動されました。]

3.2.1

water intake

process of withdrawing seawater from the source

3.2.2

surface intake

seawater collected from the open ocean above the seabed

Note 1 to entry: Surface intakes can be single purpose or collocated with a power plant as well as offshore submerged, nearshore submerged, or nearshore surface intakes.

3.2.3

subsurface intake

seawater collected via vertical wells (3.2.3.1) , infiltration galleries or other locations beneath the seabed

Note 1 to entry: Subsurface intakes can be onshore (vertical wells), including vertical beach wells or deep aquifer wells, horizontal wells, radial or collector wells, and beach infiltration galleries; or offshore wells, including horizontal drains (wells), and seabed infiltration galleries.

3.2.3.1

vertical well

well which is well-drilled straight down into the underlying rock or unconsolidated coastal aquifer system

3.2.3.2

slant well

well which is well-drilled at an angle from the horizontal into the underlying rock or unconsolidated coastal aquifer system

3.2.3.3

infiltration gallery

filtering device which is a horizontal drain made from open jointed or perforated pipes, or a blocked drain, which is laid below the water table and collects seawater

3.2.3.4

tunnelled intake

seawater collected from deep water by the tunnelled structure

Note 1 to entry: The tunnel is built over the full distance from the intake structure to the diffusers offshore.

3.3.1

pre-treatment

processes such as chlorination, filtration, coagulation, clarification, dechlorination, which may be used on feed water (3.1.4) ahead at reverse osmosis (3.4.2) membrane devices and distillation devices to minimize scaling (3.6.2) and blockage potential and to control biological activity

3.3.2

sterilization

process which inactivates or removes all living organisms (including vegetative and spore forms) as well as viruses

[SOURCE:ISO 6107:2021, 3.539]

3.3.3

dissolved air flotation

DAF

flotation process by which low density particles are removed from seawater by using fine bubbles which are produced by the reduction in pressure of a water stream saturated with air

[SOURCE:ISO 20480-4:2021, 3.2, modified — Note 1 to entry has been removed.]

3.3.4

flocculation

formation of large separable particles by aggregation of small particles; the process is usually assisted by mechanical, physical, chemical or biological means

[SOURCE:ISO 6107:2021, 3.234]

3.3.5

sedimentation

process of settling and depositing suspended solids in water under the action of gravity

3.3.6

sand filter

device used to remove suspended solids

Note 1 to entry: Sand filter is made up of layers of inert medium, usually quartz/silica sand.

3.3.7

multimedia filter

MMF

layered filtration media in a pressurized container, used to reduce the level of suspended solids (turbidity) in incoming feed water (3.1.4)

Note 1 to entry: Media layers can consist of anthracite, activated carbon, quartz/silica sand and garnet.

[SOURCE:ISO 22519:2023, 3.1.3]

3.3.8

self-cleaning filter

filtration system used to reduce the level of suspended solids (turbidity) in incoming feed water (3.1.4) , as well as automatically clean itself

Note 1 to entry: The self-cleaning filter starts automatic cleaning mechanisms according to the pre-set cleaning cycle or system differential pressure due to the accumulation of suspended solids (turbidity).

3.3.9

microfiltration

MF

pressure driven membrane-based separation process designed to remove particles and dissolved macromolecules in the approximate range of 0,05 µm to 2 µm

[SOURCE:ASTM D6161-2019, 5.1]

3.3.10

ultrafiltration

UF

pressure driven process employing a semipermeable membrane under a hydraulic pressure gradient to separate components in a solution

Note 1 to entry: The pores of the membrane are of a size smaller than 0,1 µm, which allows passage of the solvent(s) but will retain non-ionic solutes based primarily on physical size, not chemical potential.

[SOURCE:ASTM D6161-2019, 5.1, modified — part of the original definition has been moved to Note 1 to entry.]

3.3.11

cartridge filter

device used to further reject the remained foulants in the feed water (3.1.4) before reverse osmosis (RO) (3.4.2) membranes

Note 1 to entry: The purpose of the cartridge filter is to protect the RO membranes from damage.

3.4.1

high-pressure feed pump

device used to deliver feed water (3.1.4) to the reverse osmosis (3.4.2) membranes at the pressure required for membrane separation of desalinated water (3.1.5) from the seawater

3.4.2

reverse osmosis

ro

separation process where one component of a solution is removed from another component by flowing the feed stream under pressure across a semipermeable membrane that causes selective movement of solvent against its osmotic pressure difference

Note 1 to entry: RO removes ions based on electro chemical forces, colloids, and organics down to 150 molecular mass.

[SOURCE:ASTM D6161-2019, 5.1, modified — part of the original definition has been moved to Note 1 to entry.]

3.4.3

pressure vessel

container filled with reverse osmosis (3.4.2) membrane element(s)

3.4.4

booster pump

device used to deliver the water from the energy recovery device (3.4.5) to the reverse osmosis (RO) (3.4.2) membranes at pressure required for RO membrane feed water (3.1.4)

3.4.5

energy recovery device

ERD

device that uses the hydraulic pressure of the brine (3.1.7) to pressurize feed water (3.1.4) in a reverse osmosis (3.4.2) desalination unit

3.4.6

reverse osmosis train

RO train

complete reverse osmosis (3.4.2) installation, including membranes, high pressure feed pump and energy recovery device (3.4.5) operating in parallel

3.4.7

pass

process of feed water (3.1.4) being further desalinated by the reverse osmosis (3.4.2) / nanofiltration (3.4.13) membranes

Note 1 to entry: The multi-pass membrane system means the permeate from the former pass flows into the latter pass, which is usually used to filtrate the permeated water for improving the water quality.

3.4.8

stage

<membrane desalination> process of feed water (3.1.4) being further concentrated by the reverse osmosis (3.4.2) / nanofiltration (3.4.13) membranes

Note 1 to entry: The multi-stage membrane system means the concentrated water from the former stage flows into the latter stage, which is usually used to further concentrate the brine (3.1.7) for improving the recovery rate (3.1.9) .

3.4.9

single pass reverse osmosis

SPRO

single pass membrane-based process to separate dissolved ions and suspended solids

3.4.10

double pass reverse osmosis

DPRO

double pass membrane-based process to separate dissolved ions and suspended solids

3.4.11

membrane rejection rate

relative measure of how much of the target constituent that was initially in the feed water (3.1.4) is separated from the liquid by the membrane

Note 1 to entry: Rejection is generally expressed by 1 - C₂/C₁ ここで, C₁ is feed concentration and C₂ is permeate concentration. To make the guideline simple, the word “membrane” is frequently omitted depending on the context.

[SOURCE:ISO 23070:2020, 3.6]

3.4.12

permeate flux

rate at which water molecules diffuse through the membrane

Note 1 to entry: Permeate flux is expressed in terms of flow rate per unit area i.e. litre per square metre per hour (l/m²/h).

3.4.13

nanofiltration

NF

crossflow process with pore sizes designed to remove selected salts and most organics above approximately 300 molecular weight range, sometimes referred to as loose reverse osmosis (3.4.2)

Note 1 to entry: Nanofiltration is a pressure-driven membrane separation process in which particles and dissolved molecules smaller than approximately 2 nm are rejected.

[SOURCE:ASTM D6161-2019, 5.1, modified — part of the original definition has been moved to Note 1 to entry.]

3.4.14

electrodialysis

process used for the deionization of water in which ions are removed, under the influence of an electric field, from one body of water and transferred to another across an ion-exchange membrane

3.4.15

forward osmosis

process across a semipermeable membrane which is driven by osmotic pressure difference to separate dissolved solutes from feed water (3.1.4)

3.4.16

ion exchange

process by which certain anions or cations in water are replaced by other ions by passage through a bed of ion-exchange material

[SOURCE:ISO 6107:2021, 3.300]

3.4.17

membrane distillation

membrane separation process driven by the vapor pressure difference between the feed side with higher temperature and the permeate side with lower temperature

Note 1 to entry: Generally, the micro-porous hydrophobic membranes are used in membrane distillation process.

3.5.1

multi-effect distillation

MED

process of evaporation/condensation in a series of evaporators/condensers (effects) where the incoming steam condenses as fresh water on one side of heat transfer tubes, while the potential heat of condensation evaporates the seawater on the other side of the tubes; the evaporated secondary steam (3.5.9) is conducted into the next effect to repeat the above process

3.5.1.1

multi-effect distillation plant

set of interrelated or interacting units for multi-effect distillation (3.5.1) , including evaporators (3.5.1.4) , condensers (3.5.3) , vacuum equipment, instruments and meters

3.5.1.2

low-temperature multi-effect distillation

LT-MED

multi-effect distillation (3.5.1) process which usually operates at the temperature ≤ 70 °C and the absolute pressure ≤ 0,03 MPa

3.5.1.3

effect

basic unit in the multi-effect distillation plant (3.5.1.1) to complete the heat exchange between seawater evaporation and steam condensation for producing desalinated water (3.1.5)

3.5.1.4

evaporator

device used for evaporating and condensing seawater in a multi-effect distillation plant (3.5.1.1)

Note 1 to entry: The evaporator is mainly composed of heat transfer tubes, tube sheets and shells.

3.5.1.5

steam-jet vacuum pump

device that uses steam as the power to extract non-condensable gas (3.5.10) from a distillation system to form a vacuum state

3.5.1.6

thermal vapour compressor

TVC

device that uses motive steam (3.5.7) as the power to suck and inlet low-pressure steam from the distillation desalination device according to the Venturi effect, and make the mixture steam reach the pre-set pressure

Note 1 to entry: TVC is usually used in conjunction with a multi-effect distillation (MED) (3.5.1) device, which can be abbreviated as MED-TVC.

3.5.2

multi-stage flash distillation

MSF

distillation process of evaporating/condensing feed water (3.1.4) by passing through a series of flash evaporators (3.5.2.3) where the temperature and pressure are reduced stage by stage

3.5.2.1

stage

<distillation desalination> basic unit in the multi-stage flash distillation (3.5.2) plant to complete a single flashing (3.5.2.2) of feed water (3.1.4)

3.5.2.2

flashing

evaporation phenomenon caused by a sudden pressure drop sufficiently below the saturation pressure

Note 1 to entry: When the high-pressure saturated liquid enters a relatively low-pressure container, it will become a part of the saturated steam and saturated liquid under this relatively low pressure by a sudden pressure drop.

3.5.2.3

flash evaporator

device used for seawater preheating, flashing (3.5.2.2) , vapour condensing and distillate collection in multi-stage flash distillation (3.5.2)

Note 1 to entry: A flash evaporator is mainly composed of heat transfer tubes, tube sheets, flash chambers and shells.

3.5.3

condenser

device (heat exchanger) used for condensing the secondary steam (3.5.9) of the last effect (3.5.1.3) in a multi-effect distillation plant (3.5.1.1)

3.5.4

demister

device, often fitted with vapour-liquid separator vessels, to enhance the removal of liquid droplets or mist entrained in a secondary steam (3.5.9)

[SOURCE:ISO/TR 27912:2016, 3.25, modified — “vapour stream” has been replaced by “secondary steam”.]

3.5.5

gained output ratio

GOR

mass ratio of the desalinated water (3.1.5) to the heating steam per unit time

3.5.6

top brine temperature

TBT

maximum brine temperature at the outlet of the first effect (3.5.1.3) or stage (3.5.2.1)

3.5.7

motive steam

high-pressure steam that provides motive power for the thermal vapour compressor (TVC) (3.5.1.6) in a multi-effect distillation (MED) (3.5.1) -TVC device

3.5.8

primary steam

steam as a heat source of each effect in a multi-effect distillation plant (3.5.1.1)

3.5.9

secondary steam

steam produced by heating feed water (3.1.4) in an evaporator (3.5.1.4)

3.5.10

non-condensable gas

NCG

air and/or other gas which will not liquefy under the conditions of a saturated steam process

[SOURCE:ISO 11139:2018, 3.183]

3.5.11

deaeration

partial or complete removal of dissolved air from water either under natural conditions or deliberately by physical processes

[SOURCE:ISO 6107:2021, 3.152]

3.6.1

corrosion

gradual destruction or slow degradation of a substance or surface by chemical effect

Note 1 to entry: The corrosion usually happens on the surface of the seawater desalination (3.1.1) devices and pipelines.

3.6.2

scaling

build-up of precipitated salts on a surface, such as membranes, pipes, tanks, or heat transfer tubes

3.6.3

post-treatment

process such as mineralization (3.6.4) or waters blending (3.6.5) to desalinated water (3.1.5) for avoiding/minimizing pipelines corrosion (3.6.1) and making product water (3.1.6) healthy for end users

3.6.4

mineralization

process of adding minerals to desalinated water (3.1.5) to meet the requirements of product water (3.1.6) supply

3.6.5

waters blending

process of desalinated water (3.1.5) blending with other sources to meet the requirements of product water (3.1.6) supply

3.7.1

membrane cleaning

process of removing the foulants on the membrane outer and inner surface using a membrane cleaning system, with or without chemical reagents

3.7.1.1

membrane fouling

process leading to deterioration of membrane flux due to surface or internal blockage of the membrane

[SOURCE:ISO 20468-5:2021, 3.1.9, modified — the term “fouling” has been replaced by “membrane fouling”.]

3.7.1.2

transmembrane pressure

TMP

hydraulic pressure differential (net driving force) across the membrane

[SOURCE:ASTM D6161-2019, 5.1]

3.7.1.3

pressure drop

pressure change of the influent after the treatment by a reverse osmosis (3.4.2) system

[SOURCE:ISO 23070:2020, 3.9]

3.7.1.4

forward flush

forward flow of feed water (3.1.4) or permeate with or without air across a membrane (i.e. from the feed side to the permeate side)

Note 1 to entry: The forward flush is designated to remove the deposited foreign substances (foulants) from the membrane.

3.7.1.5

backward flush

reverse flow of feed water (3.1.4) or permeate with or without air across a membrane (i.e. from the permeate side to the feed side)

Note 1 to entry: The backward flush is designated to remove the deposited foreign substances (foulants) from the membrane.

[SOURCE:ISO 20468-5:2021, 3.1.1, modified — the term “backwash” has been replaced by “backward flush”; in the definition, “water” has been replaced by “feed water or permeate”.]

3.7.1.6

chemical cleaning

removal of membrane foulants accumulating on the membrane surface or within the membrane pores using a chemical reagent solution

3.7.1.7

cleaning in place

CIP

membrane cleaning (3.7.1) by impingement or circulation of flowing chemical solutions, without disassembling the membrane element (3.1.10)

3.7.1.8

pickling

removal of oxides or other compounds from the material surface of the desalination system by chemical or electrochemical action with an acid solution

3.7.2

agents dosing

dosing chemical agents to seawater desalination system (3.1.2) for maintaining the operation of the device and ensuring the product water (3.1.6) quality

3.7.2.1

biocide

disinfectant

chemical agent used to suppress the growth or kill bacteria and other microorganisms on the inner surfaces of intake pipes, equipment, tanks, distribution channels, and other structures which are in contact with the raw seawater

Note 1 to entry: The two primary categories are oxidizing biocides and non-oxidizing biocides.

3.7.2.2

flocculant

chemical agent used to bridge the molecules or colloids suspended in feed water (3.1.4) , and facilitate the agglomeration of small flocs into larger flocs

3.7.2.3

coagulant

chemical agent used to assemble the dispersed colloidal particles to form larger clumps, and enable these particles to settle down due to gravitational force

3.7.2.4

defoamer

chemical agent with surface active properties for reducing and hampering the formation of foam in the desalination processes

3.7.2.5

antiscalant

as

chemical scale inhibitor or sequestering agents that minimize the potential for scale precipitation on the reject surface of membranes and heat transfer tubes

3.7.2.6

reducing agent

chemical agent used to remove residual chlorine from the feed water (3.1.4)