WO2018103133A1 - 一种基于 lng 冷能的烟气水合物法海水淡化系统 - Google Patents

一种基于 lng 冷能的烟气水合物法海水淡化系统 Download PDF

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WO2018103133A1
WO2018103133A1 PCT/CN2016/110553 CN2016110553W WO2018103133A1 WO 2018103133 A1 WO2018103133 A1 WO 2018103133A1 CN 2016110553 W CN2016110553 W CN 2016110553W WO 2018103133 A1 WO2018103133 A1 WO 2018103133A1
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hydrate
chamber
decomposition
flue gas
gas
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French (fr)
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宋永臣
郑嘉男
杨明军
刘卫国
赵佳飞
张毅
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Dalian University of Technology
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Dalian University of Technology
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/22—Treatment of water, waste water, or sewage by freezing
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/26—Treatment of water, waste water, or sewage by extraction
    • C02F1/265—Desalination
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/108—Production of gas hydrates
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/005—Valves
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/06—Pressure conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/10—Temperature conditions for biological treatment
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the invention belongs to the field of hydrate application research and relates to a flue gas hydrate method seawater desalination system based on LNG cold energy.
  • CO 2 capture and desalination combined technology more specifically CO. 2 hydrate method seawater desalination technology.
  • the basic principle of this technology is to use CO 2 and seawater to form hydrates under certain low temperature and high pressure (heating, depressurization or a combination of the two will cause the hydrate to decompose). Due to the salt release effect, sodium and magnesium in seawater Chlorine plasma cannot enter the hydrate and remains in the solution all the time. Therefore, the hydrate is decomposed separately to obtain fresh water.
  • the invention intends to provide a flue gas hydrate method seawater desalination system based on LNG cold energy, the purpose of which is to adopt a more convenient and effective scheme for seawater desalination, and use LNG cold energy to reduce the cost input of hydrate method desalination, and simultaneously capture
  • the CO 2 is sealed and stored, effectively reducing the CO 2 content in the atmosphere, reducing the waste heat of the flue gas, and finally achieving large-scale and low-cost seawater desalination.
  • the invention intends to provide a flue gas hydrate seawater desalination system based on LNG cold energy, the purpose of which is to adopt a more effective scheme for low-cost hydrate seawater desalination, and at the same time realize CO 2 capture and LNG cold energy utilization. Finally, large-scale desalination is achieved.
  • a flue gas hydrate seawater desalination system based on LNG cold energy comprising a refrigeration system, a flue gas trapping system, a hydrate formation separation system, a hydrate decomposition system, a CO 2 circulation system and a control system;
  • the refrigeration system includes an LNG storage tank 1, a gasification chamber 11 and a circulating refrigerant to adjust the opening degree of the screw valve 18 of the LNG storage tank 1.
  • the LNG gasification amount, the LNG gasification endotherm, transfers the cold energy to the circulating refrigerant in the gasification chamber 11, and the circulating refrigerant is closed by the water pump 12, and passes through a plurality of heat exchangers. 13 respectively exchange heat with seawater and gas before hydrate formation, and directly generate hydrate formation by seawater and gas after heat exchange;
  • the flue gas trapping system comprises a flue gas source 3, a heat exchange decomposition chamber 9, a first stage generating chamber 5-1 and a gas separation chamber 6, and the flue gas source 3 is exchanged with the hydrate through the heat exchange decomposition chamber 9.
  • the heat causes the hydrate to decompose, and after exchanging heat with the circulating refrigerant, it enters the first stage generating chamber 5-1 through the air pump 15 and the check valve 20 in sequence, and forms CO 2 hydrate with seawater in the first stage generating chamber 5-1.
  • the residual gas (mainly N 2 ), the CO 2 hydrate and the residual seawater mixture are sent to the gas separation chamber 6 by the mixing pump 14 , and the butterfly valve 17 of the mixing pump 14 is automatically according to the mixing pump.
  • the hydrate formation separation system includes a second stage generation chamber 5-2 and a liquid separation chamber 7, and the CO 2 hydrate in the first stage generation chamber 5-1 is quickly entered by the mixing pump 14 after separating the residual gas.
  • the rate of newly entering seawater and CO 2 to generate CO 2 hydrate is greatly increased, and the generated large amount of CO 2 hydrate and residual seawater are all sent from the mixing pump 14 to the liquid separation chamber 7 .
  • the liquid separation chamber 7 separates the residual seawater and discharges the waste liquid through the gate valve 19, and the remaining pure CO 2 hydrate is sent from the mixing pump 14 to the evacuation type decomposition chamber 8 for decomposition; in the above process, the mixed pump 14 Controlled by the control system;
  • the hydrate decomposition system feeds the fresh water obtained by decomposing the CO 2 hydrate in the suction type decomposition chamber 8 and the heat exchange type decomposition chamber 9 into the fresh water storage tank 10, and outputs it for use, and the decomposition pressure of the suction type decomposition chamber 8 is used.
  • the decomposition temperature of the heat exchange decomposition chamber 9 is determined by the heat exchange of the smoke source 3;
  • the CO 2 cycle the pumping system pumping of formula 8 obtained by the decomposition chamber and the recuperative decomposition chamber 9 hydrate dissociation extra CO 2 was recovered CO 2 gas tank 4, CO 2 gas tank 4 for providing a first
  • the hydrate in the secondary generation chamber 5-2 generates the required CO 2 gas, and the excess CO 2 is used for storage in a conventional manner;
  • the control system is used to control the entire based LNG cold energy flue gas hydrate method seawater desalination system coordinated operation, intelligent control of each part of the periodic alternate operation, can control the opening and closing and interlocking actions of each valve and pump according to need; enter the gasification chamber through adjustment 11
  • the amount of LNG is controlled to control the temperature of the circulating refrigerant.
  • the temperature is automatically set by the control system according to the pressure of the generating chamber to ensure the smooth formation of the hydrate; the water pump 12 and the check valve are respectively required according to the requirements of the two-stage generating chamber.
  • the 20 automatically adjusts the amount of seawater to be dispensed; according to the heat capacity (gas volume * temperature) of the flue gas source 3, the amount of hydrate in the heat exchange type decomposition chamber 9 is distributed, and the remaining hydrates are distributed to the pumping type decomposition chamber 8 .
  • the LNG cold energy-based flue gas hydrate seawater desalination system recovers the hot flue gas waste heat and separates and captures the CO 2 contained therein, and the separated residual N 2 and high-concentration sea water can be used for other routes, all Some of them are resistant to high pressure carbon dioxide and high concentration seawater corrosion, and all have the function of heat preservation and pressure retention.
  • the invention has the beneficial effects of realizing CO 2 capture and seawater desalination integration, utilizing LNG cold energy to solve the problem of hydrated seawater desalination cold energy source, reasonable structure and extraordinar system; two-stage hydrate formation chamber, which solves smoke gas The CO 2 capture and the hydrate formation amount are ensured; the two hydrate decomposition chambers not only utilize the waste heat of the hot flue gas, reduce the heat discharge, but also realize the recycling and storage of CO 2 , and have a strong change of the flue gas source.
  • the carrying capacity is not affected by seasonal and environmental changes, and has great practical application value.
  • Figure 1 is a block diagram of the system of the present invention.
  • FIG. 2 is a schematic view showing the structure of the system of the present invention.
  • 1LNG storage tank 1 sea pool; 2 sea pool; 3 flue gas source; 4CO 2 gas tank;
  • liquid separation chamber 7 liquid separation chamber; 8 suction type decomposition chamber; 9 heat exchange decomposition chamber; 10 fresh water storage tank;
  • the control system starts the water pump 12 for circulating refrigerant, and at the same time sets the temperature of the refrigerant, and issues the screw valve of the LNG storage tank 1 18 opening command to adjust the amount of LNG entering the gasification chamber 11 so that the refrigerant reaches and maintains the set temperature;
  • the hot flue gas enters the heat exchange decomposition chamber 9, exchanges heat with the hydrate to be endothermicly decomposed, and then passes through the heat pump 13 through the heat pump 13 to exchange heat with the circulating refrigerant to be pre-cooled into the first stage generating chamber 5-1.
  • the seawater is pre-cooled by the water pump 12 and then introduced into the first-stage generation chamber 5-1 to generate CO 2 hydrate with the CO 2 in the cold flue gas; the residual gas after the generation, the mixture of the residual seawater and the CO 2 hydrate
  • the mixed pump 14 is fed into the gas separation chamber 6, and after the generation of the CO 2 hydrate, the gas component is mainly N 2 , and the gas separation chamber 6 extracts all the gases in the mixture, leaving the CO 2 hydrate and the residue.
  • the seawater mixture continues to be fed to the second stage generating chamber 5-2 by the mixing pump 14;
  • the seawater of the second-stage generating chamber 5-2 is the same as the source of the first stage, and the gas is supplied from the CO 2 gas tank 4, and the CO 2 is sent to the second-stage generating chamber 5-2 by the air pump 15, and the seawater and the CO 2 are both
  • the pumping type decomposition chamber 8 uses a pressure reduction method to decompose the CO 2 hydrate, and the decomposed fresh water enters the fresh water storage tank 10 through the check valve 20, and the decomposition pressure is controlled by the air pump 15, and the CO 2 gas is sent through the check valve 20
  • the CO 2 gas tank 4 is introduced to ensure continuous decomposition of the CO 2 hydrate;
  • the heat exchange decomposition chamber 9 accelerates the decomposition of the CO 2 hydrate by means of temperature rise, and the fresh water decomposed into the fresh water storage tank 10 through the check valve 20, the decomposition temperature Obtained by heat exchange with the hot flue gas 3, the decomposed CO 2 gas enters the CO 2 gas tank 4 through the pressure reducing valve 16;
  • the CO 2 stored in the CO 2 gas tank 4 is mainly used for the second stage generating chamber 5-2 hydration
  • the required CO 2 is stored in a conventional manner.
  • the above is only a basic description under the concept of the present invention, and one of the
  • the LNG cold energy flue gas hydrate method seawater desalination system is not limited to the structures and steps described in the above embodiments, and a person skilled in the art can design a similar system or base the above.
  • the partial function independent or the overall function of the LNG cold energy flue gas hydrate seawater desalination system is used in combination, and all of them are equivalent transformation or use according to the technical scheme of the present invention, and all belong to the protection scope of the present invention.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

一种基于LNG冷能的烟气水合物法海水淡化系统，属于水合物应用技术领域。利用水合物的生成捕集烟气中的CO 2，设置两级水合物生成室提高水合物量，分别采用气体分离和液体分离两部提纯CO 2水合物，分别采用换热式和抽气式两种水合物分解方式实现烟气余热的利用和CO 2的循环利用。实现CO 2捕集和海水淡化一体化，利用LNG冷能解决水合物法海水淡化冷能来源问题，结构合理、系统精妙；两级水合物生成室，既解决烟气中CO 2捕集，又保证水合物生成量；两种水合物分解室，既利用热烟气余热、减少热排放，又实现了CO 2的循环使用与封存，具备较强的烟气源变化承载能力，不受季节及环境的变化影响，具有极大的现实应用价值。

Description

一种基于 LNG 冷能的烟气水合物法海水淡化 系统
技术领域
本发明属于水合物应用研究领域，涉及一种基于 LNG冷能的烟气水合物法海水淡化系统。
背景技术
近年来，由于淡水匮乏和温室效应逐渐成为全球问题，许多国家都在进行相关的研究以解决这些问题，而最有前景的技术就是 CO2捕集与海水淡化联合技术，更确切的说是 CO2水合物法海水淡化技术。这种技术的基本原理是利用 CO2和海水在一定的低温高压下生成水合物（升温、降压或二者结合会让水合物分解），由于排盐效应的存在，海水中的钠、镁、氯等离子无法进入水合物中，会一直留存在溶液中，因此单独将水合物进行分解，即可得到淡水。目前，在已公开的专利文献和研究成果中，水合物法海水淡化技术中，产量和效率仍受水合物生成状况的限制，更重要的是此技术需要大量能量用来提供低温环境生成水合物，而 LNG（液化天然气）储存温度 -162℃，无论是存储、运输还是气化使用过程中都蕴藏了极大的冷能，完全可以用于水合物法海水淡化的制冷。因此，本发明结合 LNG冷能，使用热烟气（约 40℃，约含 20%CO2和 80%N2）中的 CO2与海水生成水合物，采用更为简便有效的方案实现淡水产率和能量利用效率的提高。
本发明拟提供一种基于 LNG冷能的烟气水合物法海水淡化系统，其目的是采用更为便利有效的方案进行海水淡化，利用 LNG冷能降低水合物法海水淡化的成本投入，同时捕集封存 CO2，有效降低大气中 CO2含量 ,减少烟气的余热排放，最终实现大规模低成本的海水淡化。
发明内容
本发明拟提供一种基于 LNG冷能的烟气水合物法海水淡化系统，其目的是采用更为有效的方案进行低成本的水合物法海水淡化，同时实现 CO2捕集以及 LNG冷能利用，最终实现大规模海水淡化。
本发明的技术方案：
一种基于 LNG冷能的烟气水合物法海水淡化系统，包括制冷系统、烟气捕集系统、水合物生成分离系统、水合物分解系统、 CO2循环系统和控制系统；
所述的制冷系统包括 LNG储罐 1、气化室 11和循环冷媒，调节 LNG储罐 1的旋拧阀 18开度改变 LNG气化量， LNG气化吸热，在气化室 11将冷能传递给循环冷媒，循环冷媒由输水泵 12实现封闭循环，并通过多个换热器 13分别与水合物生成前的海水和气体换热，换热后的海水和气体直接进行水合物生成；
所述的烟气捕集系统包括烟气源 3、换热式分解室 9、第一级生成室 5-1和气体分离室 6，烟气源 3经过换热式分解室 9与水合物换热促使水合物分解，再与循环冷媒换热后，依次通过抽气泵 15和单向阀 20进入第一级生成室 5-1，在第一级生成室 5-1中与海水生成 CO2水合物，将生成后的残留气体（主要是 N2）、 CO2水合物和残余海水混合物通过混输泵 14保压保温送入气体分离室 6，混输泵 14的蝶阀 17自动根据混输泵 14的启停而开合，混合物中的残留气体被气体分离室 6的抽气泵 15分离出去，气体分离室 6内留下的 CO2水合物和残余海水依次经过混输泵 14被立刻上送入第二级生成室 5-2；
所述的水合物生成分离系统包括第二级生成室 5-2和液体分离室 7，第一级生成室 5-1中的 CO2水合物在分离完残余气体后通过混输泵 14快速进入第二级生成室 5-2中，新进入的海水和 CO2生成 CO2水合物速率大幅提高，将生成后的大量 CO2水合物和残余海水由混输泵 14全部送至液体分离室 7，液体分离室 7将残余海水进行分离并通过闸阀 19将废液排出，剩下的纯净 CO2水合物由混输泵 14送至抽气式分解室 8进行分解；上述过程中混输泵 14由控制系统控制；
所述的水合物分解系统将抽气式分解室 8和换热式分解室 9中 CO2水合物分解得到的淡水送入淡水储罐 10，并输出使用，抽气式分解室 8的分解压力由抽气泵 15控制，换热式分解室 9的分解温度由烟气源 3换热决定；
所述的 CO2循环系统将抽气式分解室 8抽气得到的和换热式分解室 9水合物分解多出的 CO2回收到 CO2气罐 4， CO2气罐 4用于提供第二级生成室 5-2中水合物生成所需 CO2气体，多余的 CO2用于常规方式封存；
所述的控制系统用于控制整个基于 LNG冷能的烟气水合物法海水淡化系统的协调运行，智能控制各部分的周期性交替运行，能够根据需要控制各阀门、泵的开合启停与联锁动作；通过调节进入气化室 11的 LNG量，控制循环冷媒温度，温度由控制系统根据生成室的压力自动设定，保证水合物顺利生成；分别根据两级生成室的需要，通过输水泵 12和单向阀 20自动调整分配进入的海水量；根据烟气源 3热容量（气量 *温度），分配 换热式分解室 9的水合物量，其余的水合物均分配到抽气式分解室 8。
所述的基于 LNG冷能的烟气水合物法海水淡化系统，将热烟气余热回收、并分离捕集所含 CO2，分离出的残余 N2和高浓度海水可用于其他途径需要，所有部分均耐高压二氧化碳和高浓度海水腐蚀，均具有保温保压功能。
本发明的有益效果是：实现 CO2捕集和海水淡化一体化，利用 LNG冷能解决水合物法海水淡化冷能来源问题，结构合理、系统精妙；两级水合物生成室，既解决烟气中 CO2捕集，又保证水合物生成量；两种水合物分解室，既利用热烟气余热、减少热排放，又实现了 CO2的循环使用与封存，具备较强的烟气源变化承载能力，不受季节及环境的变化影响，具有极大的现实应用价值。
附图说明
图 1是本发明系统框图。
图 2是本发明系统结构示意图。
图中： 1LNG储罐； 2海水池； 3烟气源； 4CO2气罐；
5-1第一级物生成室； 5-2第二级物生成室； 6气体分离室；
7液体分离室； 8抽气式分解室； 9换热式分解室； 10淡水储罐；
11气化室； 12输水泵； 13换热器； 14混输泵； 15抽气泵；
16减压阀； 17蝶阀； 18旋拧阀； 19闸阀； 20单向阀。
具体实施方式
以下结合技术方案和附图详细叙述本发明的具体实施方式。
按照图 1原理，如图 2所示连接所述的系统结构，使用该系统进行基于 LNG冷能的烟气水合物法海水淡化，步骤如下：
控制系统启动循环冷媒的输水泵 12，同时设定冷媒温度，发布 LNG储罐 1的旋拧阀 18开度指令，调节进入气化室 11的 LNG量，从而使冷媒达到并维持设定温度；
热烟气进入换热式分解室 9，与待吸热分解的水合物进行换热，然后通过抽气泵 15流经换热器 13与循环冷媒换热预冷进入第一级生成室 5-1，同时海水通过输水泵 12预冷后通入第一级生成室 5-1，与冷烟气中的 CO2生成 CO2水合物；生成后的残留气体、残余海水和 CO2水合物的混合物被混输泵 14送进气体分离室 6，生成 CO2水合物后气体组分中主要是 N2，气体分离室 6将混合物中的气体全部抽离出来，留下的 CO2水合物和残余海水混合物继续被混输泵 14送进第二级生成室 5-2；
第二级生成室 5-2的海水与第一级来源相同，而气体由 CO2气罐 4提供， CO2被抽气泵 15送入第二级生成室 5-2，海水与 CO2均与循环冷媒换热预冷；接下来，混输泵 14将含残余海水和 CO2水合物的混合物通入液体分离室 7，液体分离室 7将混合物中的残余海水废液分离出来并通过闸阀 19排出； CO2水合物经过混输泵 14分别进入抽气式分解室 8和换热式分解室 9，进入两个分解室的 CO2水合物量由控制系统根据烟气源 3决策分配；
抽气式分解室 8采用降压方式促使 CO2水合物分解，分解得到的淡水通过单向阀 20进入淡水储罐 10，分解压力由抽气泵 15控制，将 CO2气体通过单向阀 20送进 CO2气罐 4，以保证 CO2水合物持续分解；换热式分解室 9采用升温的方式促使 CO2水合物分解，分解得到的淡水通过单向阀 20进入淡水储罐 10，分解温度由与热烟气 3换热得到，分解多出的 CO2气体通过减压阀 16进入 CO2气罐 4； CO2气罐 4储存的 CO2主要用于第二级生成室 5-2水合物生成所需，多余的 CO2进行常规方式的封存处理。
以上仅为本发明构思下的基本说明，所涉及的一种基于 LNG冷能的烟气水合物法海水淡化系统并不仅仅限于以上实施例中所述的结构和步骤，本领域技术人员可以据此设计出类似的系统或者是将所述一种基于 LNG冷能的烟气水合物法海水淡化系统中的部分功能独立或整体功能叠加使用，这些都是依据本发明的技术方案所作的等效变换或者使用，均应属于本发明的保护范围。

Claims (1)

1. 一种基于 LNG 冷能的烟气水合物法海水淡化系统，其特征在于，该烟气水合物法海水淡化系统包括制冷系统、烟气捕集系统、水合物生成分离系统、水合物分解系统、 CO2 循环系统和控制系统；
所述的制冷系统包括 LNG 储罐 (1) 、气化室 (11) 和循环冷媒，调节 LNG 储罐 (1) 的旋拧阀 (18) 开度改变 LNG 气化量， LNG 气化吸热，在气化室 (11) 将冷能传递给循环冷媒，循环冷媒由输水泵 (12) 实现封闭循环，并通过多个换热器 (13) 分别与水合物生成前的海水和气体换热，换热后的海水和气体直接进行水合物生成；
所述的烟气捕集系统包括烟气源 (3) 、换热式分解室 (9) 、第一级生成室 (5-1) 和气体分离室 (6) ，烟气源 (3) 经过换热式分解室 (9) 与水合物换热促使水合物分解，再与循环冷媒换热后，依次通过抽气泵 (15) 和单向阀 (20) 进入第一级生成室 (5-1) ，在第一级生成室 (5-1) 中与海水生成 CO2 水合物，将生成后的残留气体、 CO2 水合物和残余海水混合物通过混输泵 (14) 保压保温送入气体分离室 (6) ，混输泵 (14) 的蝶阀 (17) 自动根据混输泵 (14) 的启停而开合，混合物中的残留气体被气体分离室 (6) 的抽气泵 (15) 分离出去，气体分离室 (6) 内留下的 CO2 水合物和残余海水依次经过混输泵 (14) 被立刻上送入第二级生成室 (5-2) ；
所述的水合物生成分离系统包括第二级生成室 (5-2) 和液体分离室 (7) ，第一级生成室 (5-1) 中的 CO2 水合物在分离完残余气体后通过混输泵 (14) 快速进入第二级生成室 (5-2) 中，新进入的海水和 CO2 生成 CO2 水合物速率大幅提高，将生成后的大量 CO2 水合物和残余海水由混输泵 (14) 全部送至液体分离室 (7) ，液体分离室 (7) 将残余海水进行分离并通过闸阀 (19) 将废液排出，剩下的纯净 CO2 水合物由混输泵 (14) 送至抽气式分解室 (8) 进行分解；上述过程中混输泵 (14) 由控制系统控制；
所述的水合物分解系统将抽气式分解室 (8) 和换热式分解室 (9) 中 CO2 水合物分解得到的淡水送入淡水储罐 (10) ，并输出使用，抽气式分解室 (8) 的分解压力由抽气泵 (15) 控制，换热式分解室 (9) 的分解温度由烟气源 (3) 换热决定；
所述的 CO2 循环系统将抽气式分解室 (8) 抽气得到的和换热式分解室 (9) 水合物分解多出的 CO2 回收到 CO2 气罐 (4) ， CO2 气罐 (4) 用于提供第二级生成室 (5-2) 中水合物生成所需 CO2 气体，多余的 CO2 用于常规方式封存；
所述的控制系统用于控制整个基于 LNG 冷能的烟气水合物法海水淡化系统的协调运行，智能控制各部分的周期性交替运行，根据需要控制各阀门、泵的开合启停与联锁动作；通过调节进入气化室 (11) 的 LNG 量，控制循环冷媒温度，温度由控制系统根据生成室的压力自动设定，保证水合物顺利生成 ；分别根据两级生成室的需要，通过输水泵 (12) 和单向阀 (20) 自动调整分配进入的海水量；根据烟气源 (3) 热容量，分配换热式分解室 (9) 的水合物量，其余的水合物均分配到抽气式分解室 (8) 。
PCT/CN2016/110553 2016-12-07 2016-12-17 一种基于 lng 冷能的烟气水合物法海水淡化系统 Ceased WO2018103133A1 (zh)

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* Cited by examiner, † Cited by third party
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US11292730B2 (en) * 2018-04-24 2022-04-05 Exxonmobil Research And Engineering Company Hydrates for water desalination using iso-butane additive
CN108579361A (zh) * 2018-05-09 2018-09-28 常州大学 一种lng发电厂尾气中二氧化碳低能耗捕集装置
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6565715B1 (en) * 1999-07-12 2003-05-20 Marine Desalination Systems Llc Land-based desalination using buoyant hydrate
WO2003068685A1 (en) * 2002-02-15 2003-08-21 Kebmar As Method and device for desalination of water and removal of carbon dioxide from exhaust gases
WO2013076737A1 (en) * 2011-11-25 2013-05-30 Amit Katyal System and method for hydrate-based desalination
CN103861444A (zh) * 2014-03-21 2014-06-18 大连理工大学 一种基于水合物法的二氧化碳捕集和海水淡化联产装置及方法
CN103991985A (zh) * 2014-05-28 2014-08-20 常州大学 一种利用lng气化冷能的水合物法海水淡化装置与方法
CN105688630A (zh) * 2016-01-19 2016-06-22 辽宁石油化工大学 一种水合物与过滤膜结合分离烟气中二氧化碳的方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3724229A (en) * 1971-02-25 1973-04-03 Pacific Lighting Service Co Combination liquefied natural gas expansion and desalination apparatus and method
CN101746840B (zh) * 2009-12-22 2011-09-14 中国科学院广州能源研究所 一种利用lng冷能进行海水淡化的系统
CN104003458B (zh) * 2014-05-26 2015-11-25 上海理工大学 基于压缩式制冷循环的水合物海水淡化系统
CN203866061U (zh) * 2014-05-26 2014-10-08 上海理工大学 采用co2压缩式制冷循环的水合物海水淡化系统

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6565715B1 (en) * 1999-07-12 2003-05-20 Marine Desalination Systems Llc Land-based desalination using buoyant hydrate
WO2003068685A1 (en) * 2002-02-15 2003-08-21 Kebmar As Method and device for desalination of water and removal of carbon dioxide from exhaust gases
WO2013076737A1 (en) * 2011-11-25 2013-05-30 Amit Katyal System and method for hydrate-based desalination
CN103861444A (zh) * 2014-03-21 2014-06-18 大连理工大学 一种基于水合物法的二氧化碳捕集和海水淡化联产装置及方法
CN103991985A (zh) * 2014-05-28 2014-08-20 常州大学 一种利用lng气化冷能的水合物法海水淡化装置与方法
CN105688630A (zh) * 2016-01-19 2016-06-22 辽宁石油化工大学 一种水合物与过滤膜结合分离烟气中二氧化碳的方法

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