CN208786104U - The system for removing the steady salt of heat in organic amine liquid - Google Patents

The system for removing the steady salt of heat in organic amine liquid Download PDF

Info

Publication number
CN208786104U
CN208786104U CN201821123830.3U CN201821123830U CN208786104U CN 208786104 U CN208786104 U CN 208786104U CN 201821123830 U CN201821123830 U CN 201821123830U CN 208786104 U CN208786104 U CN 208786104U
Authority
CN
China
Prior art keywords
organic amine
amine liquid
liquid
membrane stack
electrode solution
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.)
Active
Application number
CN201821123830.3U
Other languages
Chinese (zh)
Inventor
童扬传
朱纯峰
周跃
李云龙
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.)
Sijiantong Sci & Tech Dev Co Ltd Beijing
Original Assignee
Sijiantong Sci & Tech Dev Co Ltd Beijing
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 Sijiantong Sci & Tech Dev Co Ltd Beijing filed Critical Sijiantong Sci & Tech Dev Co Ltd Beijing
Priority to CN201821123830.3U priority Critical patent/CN208786104U/en
Application granted granted Critical
Publication of CN208786104U publication Critical patent/CN208786104U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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

Landscapes

  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

The utility model relates to organic amine liquid field of purification, disclose a kind of system for removing the steady salt of heat in organic amine liquid.The system includes: organic amine liquid storage device, electrode solution storage device, desalination water storage apparatus and membrane stack, the membrane stack respectively with the organic amine liquid storage device, the electrode solution storage device and the desalination water storage apparatus, which are interconnected, to be arranged, and it is respectively formed organic amine liquid circulation loop, electrode solution circulation loop and desalination water-flow circuit, the system also includes conductivity meters and control axis, the control axis is for receiving the conductivity signal from the conductivity meter, and the reuse and discharge of the circular flow and organic amine liquid and waste liquid of the organic amine liquid circulation loop and desalination water-flow circuit are adjusted according to the conductivity signal of the conductivity meter.When the system handles organic amine liquid, zwitterion simultaneous removing in amine liquid can be reduced into alkali lye consumption and discharging of waste liquid.

Description

The system for removing the steady salt of heat in organic amine liquid
Technical field
The utility model relates to organic amine liquid field of purification, and in particular to the steady salt of heat is in a kind of removing organic amine liquid System.
Background technique
There are many contain a large amount of sour gas, such as carbon dioxide (CO in unstripped gas in petrochemical industry2), vulcanization Hydrogen (H2S), sulfur dioxide (SO2) etc., need therefrom to remove the process flow that just can enter next step after these sour gas.
Amine process is widely used in removing the sour gas in natural gas, liquefied gas and flue gas.Wherein, common organic Amine includes ethanol amine (MEA), diethanol amine (DEA), N methyldiethanol amine (MDEA), triethanolamine, N- methyl ethylenediamine, two Isopropanolamine, N, N- dibutylethanolamine, ethylenediamine, diethylamine, tetramethylethylenediamine, piperazine etc..However, in circularly removing acid During property gas, the degradation and oxidation of organic amine during high temperature regeneration, the inorganic salts carried in gas, in gas Highly acid substance etc. will lead to hot steady salt content in organic amine and increase, and the raising of the steady salt of heat can cause the foaming of organic amine liquid and pipeline The problems such as corrosion, also further promotes the degradation and deterioration of amine liquid, forms vicious circle, removes sour gas so as to cause amine liquid The ability decline of body is not available even.There is a large amount of discarded amine liquid to need to handle every year, not only processing cost is huge, Er Qiezao At the wasting of resources.
To solve the above-mentioned problems, the prior art is usually to be carried out at purification after filtering amine liquid for desulphurization with ion-exchange Reason.
For example, CN102125803A discloses a kind of purification method of amine liquid inferior, method includes the following steps: (1) The filtering of solid impurity: the solid impurity of amine liquid inferior is filtered, wherein the filtering by the filter medium in fixed bed Medium is one of molecular sieve, active carbon and amberplex or a variety of；(2) it the exchange removing of acid ion: will mix Resin be seated in ion exchange column, through filtered amine liquid by mixed type ion exchange resin, be 1- in air speed 50h-1, temperature be 10-50 DEG C at realize acid ion exchange removing；(3) regeneration of filter medium and exchanger resin: by amine liquid It is excessively high by the pressure drop of filter medium, when air speed is too low, it is filtered the regeneration or replacement of medium, so as to the smooth mistake of amine liquid Filter reduces filtration time；When the inlet and outlet amine liquid pH value of exchange resin tower is close, ion exchange resin is carried out again Raw, the air speed for carrying out regeneration of ion-exchange resin is 1-50h-1, temperature be 10-50 DEG C；Resin after regeneration is recycled.
However, handling amine liquid using the above method, it is typically only capable to remove solid particle and heat stable salt therein Anion, and (such as the Na of the cation in amine liquid can not be removed+、K+、Ca2+、Mg2+Deng).Moreover, ion-exchange can consume greatly The alkaline solution (such as NaOH) of amount, discharges a large amount of strong basicity waste water, and in circulation desalination processes, the discharge amount of waste water is very To reaching 1-2 times of system amine liquid measure, the COD of waste water is very high, can not be effectively treated at present.
Utility model content
The purpose of this utility model is to overcome chemical agent consumptions in the steady salt technology of existing ion exchange removing amine liquid heat Greatly, waste liquid discharging amount is big and is difficult to take off decationizing defect, provides the system of the steady salt of heat in a kind of removing organic amine liquid and adopts The method for handling the organic amine liquid containing the steady salt of heat with the system, the system have desalting ability strong, are suitable for handling a variety of Organic amine liquid containing the steady salt type of different heat, it is easy to assembly, it is increasingly automated, save human cost.At the system Organic amine liquid of the reason containing the steady salt of heat not only may be implemented the simultaneous removing of zwitterion in amine liquid and removing depth is high, moreover it is possible to It greatly reduces or does not consume lye, waste liquid discharging amount is low, enhances the reusable service life of organic amine liquid.
To achieve the goals above, the utility model provides a kind of system for removing the steady salt of heat in organic amine liquid, the system It include: organic amine liquid storage device, electrode solution storage device, desalination water storage apparatus, membrane stack and control axis, wherein described Membrane stack is respectively communicated with the organic amine liquid storage device, the electrode solution storage device and the desalination water storage apparatus；It is described Membrane stack is provided at least one organic amine liquid import, the outlet of organic amine liquid, waste liquid import, waste liquid outlet, electrode solution import and electricity The outlet of pole liquid；The first conductivity meter and the second conductivity are respectively arranged at organic amine liquid exit and the waste liquid outlet Instrument, for monitoring the liquid electric conductivity at organic amine liquid exit and the waste liquid outlet；Organic amine liquid exit The first regulating valve, the desalination water storage apparatus are provided on Location Detection of Medium Transportation Pipeline between to the organic amine liquid storage device The second regulating valve is provided on Location Detection of Medium Transportation Pipeline between to the waste liquid entrance；The system also includes control axis, For receiving the conductivity signal from first conductivity meter and the second conductivity meter, and according to first conductivity meter The aperture of first regulating valve and second regulating valve is adjusted with the conductivity signal of the second conductivity meter.
Rarely have in the method for the existing steady salt of amine liquid removing heat and be related to the removing of cation, however, cation is in organic amine (as more than 1000ppm) after middle accumulation to a certain extent, the desulfuration efficiency of desulfurization organic amine liquid can be greatly influenced.For example, working as When being used to remove the hydrogen sulfide in liquefied gas for the amine liquid containing a large amount of sodium ions, hydrogen sulfide content liter in poor amine liquid will cause Height, the even de- rear liquefied gas sulfur content of desulfuration of liquefied gas depth decline is exceeded, and harmfulness has been even more than hot steady salt anionic. It is conventional theory that amine liquid itself should be easy to act on cation exchange resin in aqueous solution, therefore, if using sun Ion exchange resin removes cation, then forming competition commutative relation during removing cation, causes amine liquid sheet A large amount of losses of body, are unfavorable for industrialized production, therefore, how effectively to remove the skill that the cation in amine liquid is always this field Art problem.In order to avoid cations it is excessive caused by influence, currently used method is the fresh organic amine of replacement, discharge Processing deteriorates serious organic amine, but will lead to the raising of operating cost, the pollution of environment and the waste of resource in this way.
The inventor of the utility model has found that the organic amine containing hot steady salt is in electrodialytic effect after further investigation Under, the charged particle in hot steady salt can be made to generate directional migration and constantly separated, be concentrated and taken off into different compartments It removes, to realize the purification of organic amine liquid.However, the steady salinity of heat in organic amine liquid is continuous with the progress of purification process It reducing, the conductivity of organic amine liquid can be gradually reduced, theoretically, and when hot steady salinity is reduced to 0 or when close to 0, organic amine liquid In almost without transportable charged particle, cause organic amine liquid electric conductivity low.Amine liquid is indoor in electrodialytic process has The decline of machine amine liquid electric conductivity will lead to serious consequence, such as: (1) organic amine liquid occurs to ionize and enters demineralized water compartment and cause The loss of organic amine liquid is unable to complete further desalination；(2) it will cause current efficiency reduction, electric energy is further converted to heat Can, cause organic amine liquid temperature to increase, irreversible damage is caused to amberplex.In order to solve this problem, this is practical It is novel inventors have found that ion exchange resin is packed into electrodialytic amine liquid compartment, under organic amine liquid electric conductivity When drop even cannot be conductive, ion exchange resin plays a role as conducting medium, can effectively facilitate electrodialytic process into Row improves electrodialysis desalination efficiency.In addition, control axis is arranged in the system, the steady salt of heat in organic amine liquid may be implemented The full-automatic of subtractive process carries out, and the organic amine liquid of the steady salt of removing heat to be obtained and the demineralized water of the steady salt of enrichment heat are full respectively The organic amine liquid recycling that can be purified automatically when foot recycling and discharge standard and/or discharging of waste liquid, the recycling of organic amine liquid And/or system carries out fluid infusion to organic amine liquid and/or demineralized water automatically after discharging of waste liquid, whole process is not necessarily to manual intervention, greatly Human cost is saved.Therefore, system provided by the utility model is high to the removing depth of the steady salt of heat in organic amine liquid, automation Degree is high, effectively reduces operating cost, improves the desulfuration efficiency of organic amine liquid.
Other features and advantages of the utility model will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Fig. 1 is used in removing organic amine liquid provided by the utility model when membrane stack is yin-yang membrane stack at the steady salt system of heat The flow diagram of organic amine liquid of the reason containing the steady salt of heat；
Fig. 2 is the structure and working principle schematic diagram that membrane stack is bipolar membrane stack in the utility model.
Description of symbols
1, organic amine liquid storage device 2, electrode solution storage device 3, desalination water storage apparatus
4, membrane stack 5, control axis 61, the first regulating valve
62, the second regulating valve 63, third regulating valve 64, the 4th regulating valve
65, the 5th regulating valve 66, the 6th regulating valve 67, the 7th regulating valve
71, organic amine liquid circulating pump 72, electrode solution circulating pump 73, desalination water-circulating pump
81, organic amine liquid tank gage 82, demineralized water tank gage 91, the first conductivity meter
92, the second conductivity meter A, the first amberplex B, the second amberplex
C, third amberplex I-1, anode chamber I-2, cathode chamber
II, amine liquid chamber III, waste liquid chamber
Specific embodiment
The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more New numberical range, these numberical ranges should be considered as specific open herein.
The utility model first aspect provides a kind of system for removing the steady salt of heat in organic amine liquid, as shown in Figure 1, the system It include: organic amine liquid storage device 1, electrode solution storage device 2, desalination water storage apparatus 3, membrane stack 4 and control axis 5, wherein The membrane stack 4 is respectively communicated with the organic amine liquid storage device 1, the electrode solution storage device 2 and demineralized water storage dress Set 3；The membrane stack 4 is provided at least one organic amine liquid import, the outlet of organic amine liquid, waste liquid import, waste liquid outlet, electrode solution Import and electrode solution outlet；91 He of the first conductivity meter is respectively arranged at organic amine liquid exit and the waste liquid outlet Second conductivity meter 92, for monitoring the liquid electric conductivity at organic amine liquid exit and the waste liquid outlet；It is described to have The first regulating valve 61, institute are provided on machine amine liquid exit to the Location Detection of Medium Transportation Pipeline between the organic amine liquid storage device 1 It states and is provided with the second regulating valve 62 on desalination water storage apparatus 3 to the Location Detection of Medium Transportation Pipeline between the waste liquid entrance；It is described System further includes control axis 5, for receiving the conductivity from first conductivity meter 91 and/or the second conductivity meter 92 Signal, and adjust described first according to the conductivity signal of first conductivity meter 91 and/or the second conductivity meter 92 and adjust The aperture of valve 61 and/or second regulating valve 62.
According to the utility model, the control axis 5 is preferably automatic control device and is realized by programmable software man-machine Interface interaction, the control axis 5 can be believed according to the conductivity of first conductivity meter 91 and/or the second conductivity meter 92 Number variation, the aperture of the first regulating valve 61 and/or second regulating valve 62 described in auto-control, thus realize automatic monitoring and Control the flow and circulation and emission frequency of the organic amine liquid to be processed and/or demineralized water.
According to the utility model, it is preferable that the conductance of organic amine liquid may be set according to actual conditions in the control axis 5 Rate signal difference or conductivity signal value, the conductivity signal difference measured when first conductivity meter 91 or conductivity signal Value reaches the setting conductivity signal difference or the setting conductivity signal value, has illustrated the organic amine liquid to be processed Reach desalination standard, open the third regulating valve 63 being arranged on the export pipeline of organic amine liquid, that treated is organic by up to standard Amine liquid is exported to organic amine liquid reclaiming system.
According to the utility model, as shown in Figure 1, the membrane stack 4 includes anode plate, the yin for being oppositely arranged on 4 both ends of membrane stack Pole plate and the mould group containing multiple amberplexes being arranged between the anode plate and cathode plate；The anode plate with it is described Region between mould group forms anode chamber I-1, and the region between the cathode plate and the mould group forms cathode chamber I-2；It is described Multiple amberplexes are separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately in the mould group；It is adjacent Two amberplexes ion-selective permeability it is different；In the heteropleural of each amine liquid chamber II, the organic amine liquid is set The waste liquid import and waste liquid outlet is arranged in the heteropleural of each waste liquid chamber III, described in import and the outlet of organic amine liquid The electrode solution liquid outlet and electrode solution outlet is respectively set in the heteropleural of anode chamber I-1 and cathode chamber I-2；
The organic amine liquid inlet communication of the amine liquid chamber II of the liquid outlet and membrane stack 4 of the organic amine liquid storage device 1 Setting, the organic amine liquid outlet of the amine liquid chamber II of the inlet and membrane stack 4 of the organic amine liquid storage device 1 are set It sets, forms closed circuit, become organic amine liquid circulation loop；
The electrode solution of the electrode solution liquid outlet of the electrode solution storage device 2 and the anode chamber I-1 and cathode chamber I-2 into Mouth connection setting, the electrode of the electrode solution inlet of the electrode solution storage device 2 and the anode chamber I-1 and cathode chamber I-2 The setting of liquid outlet, forms closed circuit, becomes electrode solution circulation loop；
The waste liquid inlet communication of the demineralized water liquid outlet of the desalination water storage apparatus 3 and the waste liquid chamber III are arranged, institute It states the demineralized water inlet of desalination water storage apparatus 3 and the waste liquid outlet of the waste liquid chamber III is connected to setting, formation is closed back Road becomes desalination water-flow circuit.
According to the utility model, in order to remain to the membrane stack 4 when the decline of organic amine liquid conductivity even cannot be conductive Electrodialytic process is persistently carried out, improves the membrane stack 4 to the desalting efficiency of the steady salt of heat in organic amine liquid, under preferable case, institute It states each of to be separated out in membrane stack 4 between two amberplexes of the amine liquid chamber II and can also load amberlite Rouge；The ion exchange resin can be storng-acid cation exchange resin and/or strong-base anion-exchange resin.
According to the utility model, the storng-acid cation exchange resin can be macroporous type strongly acidic cation exchange tree Rouge and/or gel-type strongly acidic cation exchange resin, the cation in the storng-acid cation exchange resin, which can be, appoints It anticipates a kind of cation, such as organic cation (such as quaternary ammonium cation), alkali metal ion (Na+、K+), alkaline-earth metal ions (such as Mg2 +、Ca2+), transition metal ions (such as Cu2+、Fe3+、Cr3+、Zn2+、Co2+、Ni2+Deng).
According to the utility model, the strong-base anion-exchange resin can be macroporous type strong alkalinity anion exchange tree Rouge and/or gel type strong basic anion exchange resin, the anion in the strong-base anion-exchange resin, which can be, appoints It anticipates a kind of anion, such as SO4 2-、NO3 -、Cl-、HCO3 -、OH-Deng.
According to the utility model, when the organic amine liquid using the system for removing the steady salt of heat in organic amine liquid for processing When middle no metal cation, the ion exchange resin is preferably strong-base anion-exchange resin, and more preferably hydrogen-oxygen type is strong Alkalescence anion-exchange resin is most suitable for stablizing performance ionic conduction in alkaline solution because organic amine liquid is alkaline solution What is acted on is the strong-base anion-exchange resin of hydrogen-oxygen type；It is used for when using the system for removing the steady salt of heat in organic amine liquid In the organic amine liquid of processing contain metal cation when, the ion exchange resin be preferably strong-base anion-exchange resin and The mixture of storng-acid cation exchange resin, more preferably hydrogen-oxygen type strong-base anion-exchange resin and sodium form highly acid sun The body of the dosage of the mixture of ion exchange resin, the strong-base anion-exchange resin and storng-acid cation exchange resin Product ratio can be 0.5-2:1.
According to the utility model, the dosage of the ion exchange resin is not particularly limited, as long as can be in organic amine The electric conductivity decline of liquid plays electric action when even cannot be conductive, under preferable case, the ion exchange resin Dosage fills up each amine liquid chamber II enough.
According to the utility model, the electrode solution is electrolyte solution, and the concentration of the electrolyte solution can be 3-10 The solute of weight %, preferably 4-6 weight %, the electrolyte solution can be but not limited to sodium sulphate, sodium chloride, nitric acid One of sodium, sodium acetate, potassium chloride, sodium hydroxide, sulfuric acid, hydrochloric acid, nitric acid are a variety of, and main purpose is conductive, it is ensured that There are enough ions to pass in and out, improves current efficiency.
According to the utility model, the membrane stack 4 can be yin-yang membrane stack or bipolar membrane stack, adjacent two in the membrane stack 4 The different amberplex of a selective penetrated property includes the first amberplex A and the second amberplex B, when the membrane stack 4 When for yin-yang membrane stack, the first amberplex A and the second amberplex B is respectively anion-exchange membrane or cation is handed over Change film；When the membrane stack 4 is bipolar membrane stack, the first amberplex A and the second amberplex B are respectively anion Exchange membrane or Bipolar Membrane.
It may include that multiple groups ion is handed over when the membrane stack 4 is yin-yang membrane stack, in the membrane stack 4 according to the utility model Film is changed, every group of amberplex includes a cation-exchange membrane and an anion-exchange membrane, forms a repetitive unit, more The repetitive unit that group amberplex is formed is separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately.It is described The arrangement mode of the different amberplex of 4 intermediate ion selective penetrated property of membrane stack can be the row of the yin-yang membrane stack of this field routine Mode for cloth, for example, the arrangement mode of 4 intermediate ion exchange membrane of the membrane stack can with as shown in Figure 1, in the membrane stack 4, described first Amberplex A is cation-exchange membrane, and the second amberplex B is anion-exchange membrane, in the mould heap 4, from Anode plate to cathode plate direction, the mould group successively include in the multiple anion-exchange membrane B and sun being periodically arranged alternately from Proton exchange A, each anion-exchange membrane B and cation-exchange membrane A form a repetitive unit, and multiple groups amberplex is formed Repetitive unit be separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately.
It may include that multiple groups ion is handed over when the membrane stack 4 is bipolar membrane stack, in the membrane stack 4 according to the utility model Film is changed, every group of amberplex includes a Bipolar Membrane and an anion-exchange membrane, forms a repetitive unit, multiple groups ion The repetitive unit that exchange membrane is formed is separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately.In the membrane stack 4 The arrangement mode of the different amberplex of ion-selective permeability can be the arrangement mode of the bipolar membrane stack of this field routine, For example, the arrangement mode of the 4 intermediate ion exchange membrane of membrane stack can be with as shown in Fig. 2, in the mould heap 4, first ion Exchange membrane A is Bipolar Membrane, and the second amberplex B is anion-exchange membrane, and the membrane stack 4 further includes third ion exchange Film C, the third amberplex C are cation-exchange membrane, are disposed proximate to the anode plate, in the mould heap 4, from For third amberplex C to cathode plate direction, the mould group successively includes in the multiple anion exchanges being periodically arranged alternately Film B and Bipolar Membrane A, each anion-exchange membrane B and Bipolar Membrane A form a repetitive unit, what multiple groups amberplex was formed Repetitive unit is separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately.
According to the utility model, the Bipolar Membrane is by a cation-exchange membrane and a compound system of anion-exchange membrane At yin, yang film cluster ion exchange membrane.The characteristics of Bipolar Membrane is anions and canons exchange under the action of DC electric field The H of the compound interlayer of film2O is dissociated into H+And OH-And respectively by cavity block and anode membrane, as H+And OH-Ion source, working principle is such as Shown in Fig. 2.
According to the utility model, contain when using the system processing provided by the utility model for removing the steady salt of heat in organic amine liquid When having in the organic amine liquid of hot steady salt containing a large amount of strong cations, the membrane stack 4 can be yin-yang membrane stack；When described containing hot steady When in the organic amine liquid of salt without metal cation, the membrane stack 4 can be yin-yang membrane stack or bipolar membrane stack, preferably Bipolar Membrane Heap, when in the organic amine liquid that the membrane stack is containing hot steady salt without metal cation, when the membrane stack 4 is yin-yang membrane stack, institute The system of stating further includes lye input unit, inputs lye into the organic amine liquid to be processed, neutralizes in organic amine liquid to be processed Acidic materials, make to be enriched with strong cation in the organic amine liquid to be processed, in order to avoid leading to the removing of organic amine radical ion, cause The loss of organic amine liquid.
According to the utility model, organic amine liquid export pipeline is also connected in the organic amine liquid circulation loop, being used for will The organic amine liquid of the steady salt of removing heat is exported to organic amine liquid reclaiming system, is provided with third tune on the organic amine liquid export pipeline Valve 63 is saved, is also connected with waste liquid outlet pipeline in the desalination water-flow circuit, for the demineralized water conduct of hot steady salt will to be enriched with Outside discharging of waste liquid to the system, the 4th regulating valve 64 is provided on the waste liquid outlet pipeline, the control axis 5 is also used to The conductivity signal from first conductivity meter 91 and/or the second conductivity meter 92 is received, and according to first conductance The conductivity signal of rate instrument 91 and/or the second conductivity meter 92 adjusts the third regulating valve 63 and/or the 4th regulating valve 64 aperture.When the conductivity signal of first conductivity meter 91 and/or the second conductivity meter 92 meets organic amine liquid respectively When reuse standard and/or discharging of waste liquid standard, the control axis 5 controls the third regulating valve 63 and/or described respectively Four regulating valves 64 open opportunity and/or aperture.
According to the utility model, first circulation pump 71 is provided in the organic amine liquid circulation loop, the electrode solution is followed Loop back path is provided with second circulation pump 72, is provided with third circulating pump 73 in the desalination water-flow circuit, is respectively used to institute The amine liquid chamber II that the Matter Transfer in organic amine liquid storage device 1 is pumped into membrane stack 4 is stated, by the material in electrode solution storage device 2 Circulation is pumped into the anode chamber I-1 and cathode chamber I-2 of membrane stack 4, and the Matter Transfer in desalination water storage apparatus 3 is pumped into membrane stack 4 In waste liquid chamber III.Preferably, frequency conversion is additionally provided in the first circulation pump 71, second circulation pump 72 and third circulating pump 73 Device, for controlling the switch and pump speed of each pump.It is highly preferred that the first circulation pump 71, second circulation pump 72 and third are followed The starting speed of ring pump 73 is identical, and the first circulation pump 71, second circulation pump 72 and third circulating pump 73 are normal from starting to The time of operating is 20-60s, more preferably 30-40s, the first circulation pump 71, second circulation pump 72 and third circulating pump 73 It is 0-20s, more preferably 5-10s from running well the time thoroughly stopped.In addition, the frequency converter is by controlling described the The operating frequency of one circulating pump 71, second circulation pump 72 and third circulating pump 73, to adjust the flow velocity that each material enters membrane stack 4, Flow velocity to ensure each material is controllable.
Preferably, in the connecting pipeline of the respective compartment of each circulating pump to membrane stack 4, it is additionally provided with filter, it is described The setting quantity of filter can be one or more, to remove the solid particulate matter in organic amine liquid, demineralized water and electrode solution.
According to the utility model, the solid particulate matter in organic amine liquid, demineralized water and electrode solution is in respective cyclic process Dust, fine particle, equipment corrosion cast, degradation coking material, reaction precipitate of carrying etc..In order to remove above-mentioned solid Grain object, it is highly preferred that the filter is filter cartridge type filter, filtration core is that pp cotton folds cotton core, and filtering accuracy is that 0.1-1 is micro- Rice.
It is further preferred that the filter outlet is additionally provided with differential manometer, to section in the filter core gap of the filter State is stayed to be monitored.
It is further preferred that being additionally provided in the connecting pipeline of the respective compartment in each circulating pump to membrane stack 4 Flowmeter, the flowmeter can be one or more, be provided with cutout detection device on the flowmeter.Membrane stack 4 is being powered Heat can be generated in the course of work, the heat of generation is carried over the membrane stack 4 with the circulation of each material and is released, when material is disconnected When stream, no Flow of Goods and Materials cools down to membrane stack, and the heat in membrane stack 4 will continue to accumulate, and causes material in membrane stack 4 gradually Heating, or even boiling easily cause the overheat of membrane stack 4 even to burn, and the cutout detection device can effectively detect each circulation loop The flow regime of material in middle pipeline, when material cut-off in a certain pipeline, the cutout detection device signal that can will stop is anti- It feeds control axis 5, control system cuts off the power supply of membrane stack 4, avoids membrane stack 4 and is persistently powered and generates overheating problem.
According to the utility model, the import of organic amine liquid, waste liquid import and the electrode solution entrance of the membrane stack 4 are respectively set There are heat exchanger and thermometer, the temperature of the material for regulating and controlling to enter the membrane stack 4.Preferably, after heat exchanger exchanges heat, enter The temperature of charge of membrane stack 4 is 5-35 DEG C, preferably 15-25 DEG C.If the temperature of charge for flowing into membrane stack 4 is excessively high, can destroy described Effective ion cation exchange groups in first amberplex A and the second amberplex B, or even destroy first ion exchange The structure of film A and the second amberplex B may result in each material if the temperature of charge for flowing into membrane stack 4 is too low Salt crystallization or water freezing easily cause the deformation of the first amberplex A and the second amberplex B, or even described in destruction The structure of first amberplex A and the second amberplex B, cause the liquid in different compartments to be ganged up, and cause the film The loss of the desalting ability decline and organic amine liquid of heap 4.
According to the utility model, which is also provided with lye input unit, the conveying of the lye input unit Pipeline accesses the organic amine liquid storage device 1.It is provided with the 7th regulating valve 67 on the feed-line of the lye input unit, The input opportunity of lye and flow in the lye input unit are adjusted for the organic amine liquid type according to actual treatment.According to The utility model, the lye can be but not limited to sodium hydroxide and/or potassium hydroxide, lack when in organic amine liquid to be processed In the case where cation, it can avoid according to the actual situation after supplementing organic amine liquid further according to lye is required supplementation in desalination The loss of organic amine liquid is caused in the process.
According to the utility model, which is additionally provided with inert gas access device, the inert gas access device Feed-line is respectively connected to the organic amine liquid storage device 1, electrode solution storage device 2 and desalination water storage apparatus 3, to each Storage device in circulation loop carries out inertia sealing gland, it is ensured that amine liquid etc. completely cuts off air in respective circulating tank, will not be by oxygen Change.Preferably, the inert gas is nitrogen.
According to the utility model, it is additionally provided with cleaning device in the membrane stack 4, first ion described in the membrane stack 4 When exchange membrane A and/or the second amberplex B electrodialysis efficiency decline or is contaminated, to the first amberplex A And/or second amberplex B cleaned, keep the high desalination efficiency of the membrane stack 4.
Preferably, organic amine liquid tank gage 81, the demineralized water storage are additionally provided on the organic amine liquid storage device 1 It is additionally provided with demineralized water tank gage 82 on device 2, is respectively used to detect the organic amine liquid storage device 1 and the demineralized water is deposited Then the liquid level signal of the two is sent to the control axis 5 by the liquid level in storage device 2, the control axis 5 is according to described The liquid level signal of organic amine liquid tank gage 81 and/or demineralized water tank gage 82, the 5th adjusted on the amine liquid intake pipeline adjust Aperture and the switch opportunity of valve 65 and/or the 6th regulating valve 66 on the demineralized water intake pipeline are saved, and then is had described in control The fluid infusion dosage and flow velocity of machine amine liquid storage device 1 and the desalination water storage apparatus 2；The control axis 5 can also basis The liquid level signal of the organic amine liquid tank gage 81 and/or demineralized water tank gage 82 further controls the third regulating valve 63 And/or the 4th regulating valve 64 aperture and switch opportunity, organic amine liquid in Collaborative Control organic amine liquid circulation loop and/or remove The loop start of waste liquid or stopping and circular flow in brine recycling circuit.
According to the utility model, for the ease of installing and simplifying operation, the system is preferably skid-mounted system.
The utility model second aspect is provided a kind of handled using the system above-mentioned for removing the steady salt of heat in organic amine liquid and contained There is the method for the organic amine liquid of hot steady salt, the method includes organic amine liquid to be processed is introduced the system by external pipeline Organic amine liquid storage device 1, demineralized water is introduced in the desalination water storage apparatus 3 of the system, by electrode solution storage device 2 In be passed through electrode solution, organic amine liquid circulation is then pumped into the amine liquid chamber II of the membrane stack 4, the demineralized water is stored and is filled The waste liquid chamber III that the desalination water-circulating pump in 3 enters the membrane stack 4 is set, the electrode solution in electrode solution storage device 2 is recycled respectively It is pumped into the anode chamber I-1 and cathode chamber I-2 of the membrane stack 4；By the anode plate and cathode plate of the membrane stack 4 respectively with power supply just Pole is connected with cathode, and the organic amine liquid to be processed for making circulation be pumped into the membrane stack 4 carries out the steady salt removing processing of heat, obtains removing heat The demineralized water of the organic amine liquid of steady salt and the hot steady salt of enrichment, organic amine liquid and the steady salt of enrichment heat of the steady salt of removing heat to be obtained When demineralized water meets recycling and discharge standard respectively, the organic amine liquid of the steady salt of removing heat obtained after processing is delivered to organic amine Liquid reclaiming system, using the demineralized water of the steady salt of enrichment heat obtained after processing as discharging of waste liquid to the system outside.
According to the utility model, it is preferable that the power supply that the anode plate and cathode plate with membrane stack 4 are connect is flame proof direct current Power supply.
According to the utility model, the current density generated after the anode plate and cathode plate connection power supply can be according to wait locate The conductivity of the steady salinity of heat and/or the organic amine liquid in the organic amine liquid of reason carries out selection setting, for example, when it is described to When the steady salinity of heat is 0.5-10 weight % in processing organic amine liquid, or when the conductivity of the organic amine liquid to be processed is 1- When 20ms, the current density can be 5-400mA/cm2.The voltage and current of the power supply, can be according in the membrane stack 4 Membrane area set, as long as by the current density control in 5-400mA/cm2In the range of.In the membrane stack 4 The quantity of amberplex can be 20-200 group, and every group of amberplex includes two different ions of ion-selective permeability Exchange membrane forms a repetitive unit, and e.g., when membrane stack 4 is yin-yang membrane stack, one group of amberplex includes that a cation is handed over Film and an anion-exchange membrane are changed, when membrane stack 4 is bipolar membrane stack, one group of amberplex includes an anion-exchange membrane With a Bipolar Membrane.When membrane stack 4 is respectively yin-yang membrane stack or bipolar membrane stack, the working principle and its intermediate ion of the membrane stack 4 The arrangement mode of the different amberplex of selective penetrated property is as previously mentioned, details are not described herein.4 intermediate ion of the membrane stack exchange The size of film meets concerned countries and professional standard, and the amberplex for industrially commonly using 400mm × 800mm assembles membrane stack, The amberplex of useful 200mm × 400mm assembles membrane stack, and the utility model is not limited to the membrane stack of above two size.
According to the utility model, the organic amine liquid to be processed by anode plate and cathode plate respectively with power supply just When the membrane stack 4 that pole is connected with cathode, the charged particle in the steady salt of heat in organic amine liquid is under the driving of applying direct current electric field, benefit With the difference of the first amberplex A and the second amberplex B ion-selective permeability having, i.e. cation can penetrate Cation-exchange membrane, anion can penetrate anion-exchange membrane, cannot then pass through on the contrary, uncharged organic amine liquid molecule Can not be mobile by anion and cation exchange membrane, and stay in corresponding amine liquid chamber II, in organic amine liquid during circulating, The constantly steady salt of removing heat, and the charged ion in the steady salt of heat is then moved in corresponding waste liquid chamber III, in the recycle stream of demineralized water It during dynamic, is removed from organic amine liquid, thus the purpose of realizing the desalination of organic amine liquid, concentration, purification or purifying.In addition, The H of the compound interlayer of anions and canons exchange membrane in Bipolar Membrane2O is dissociated into H+And OH-And respectively by cavity block and anode membrane, as H+With OH-Ion source is generated when the steady salt of the heat contained in organic amine liquid to be processed is without metal cation using the Bipolar Membrane H+Acid is formed in conjunction with the steady salt anionic of heat removed in organic amine liquid, is enriched in demineralized water and is ultimately formed waste liquid and be disposed to Outside the system.
Organic amine liquid described in the utility model is existing for molecular forms in aqueous solution, itself without electronics, Electric conductivity leans on the steady salt of heat therein completely, however, the steady salinity of heat in organic amine liquid constantly drops with the progress of purification process Low, the conductivity of organic amine liquid can be gradually reduced, theoretically, when hot steady salinity is reduced to 0 or when close to 0, in organic amine liquid Almost without transportable charged particle, causing organic amine liquid electric conductivity to reduce so even can not be conductive.At this point, if institute Membrane stack 4 is stated still to be powered, then because amine liquid chamber II in organic amine liquid electric conductivity decline cause electric current can not by or Energization is obstructed, and will will cause serious consequence in this way, as: (1) the ionization of organic amine liquid causes organic amine liquid into waste liquid chamber III Loss, is unable to complete further desalination；(2) it will cause current efficiency reduction, electric energy is further converted to thermal energy, causes organic Amine liquid temperature increases, and causes irreversible damage to amberplex.Discharging conductivity by setting organic amine liquid can evade The above problem discharges it into organic amine liquid reclaiming system not when the conductivity of organic amine liquid not being reduced to 0 or close to 0, But steady continuous removing of the salt Jing Guo the utility model method of heat in organic amine liquid, always having makes hot steady salt reach low-down Degree can only stop the steady salt of removing heat then surely salt will will appear above-mentioned consequence at this point, once removing heat.That is, heat is steady Salinity can not be reduced to close to 0 or reach 0 degree, in order to solve this problem, it is preferable that in electrodialytic amine liquid chamber II In be packed into ion exchange resin, when the decline of organic amine liquid electric conductivity even cannot be conductive, ion exchange resin is as leading Dielectric plays a role, and can effectively facilitate the progress of electrodialytic process, improves electrodialysis desalination efficiency and desalination depth.
According to the utility model, selection and the dosage of the ion exchange resin are as previously mentioned, details are not described herein.
According to the utility model, the organic amine liquid to be processed can be the monoethanolamine containing hot steady salt, contain heat surely The diethanol amine of salt, the N methyldiethanol amine containing hot steady salt, the triethanolamine containing hot steady salt, the N- first containing hot steady salt Base ethylenediamine, the diisopropanolamine (DIPA) containing hot steady salt, the N containing hot steady salt, N- dibutylethanolamine, the second two containing hot steady salt At least one of amine, the diethylamine containing hot steady salt, the tetramethylethylenediamine containing hot steady salt, piperazine containing hot steady salt.
For example, oil refinery liquefied gas desulfurization often uses MDEA as desulfurizing agent, desulfurizing agent meeting portion during recycling Degradation oxidation is divided to generate formate, acetate, the sulfide that desulfurization generates can also be oxidized to sulfate radical, inferior sulfate radical, thio sulphur Acid group etc., these anion can be stabilized at a temperature of desulfurizer regeneration, be the steady salt (HSS) of so-called heat, the steady salt of heat Can constantly add up in amine liquid, lead to the foaming of amine liquid, color burn and corrosion, these further promote amine liquid deterioration and Degradation forms vicious circle, final to influence amine liquid desulfurization depth and desulfuration efficiency.What is more, some refineries due in this way or Such reason can introduce strong cation (such as Na in amine liquid+、K+、Ca2+、Mg2+Deng), strong cation can in sweetening process shape At the sulfide of thermal stability, causes poor amine liquid hydrogen sulfide content to increase, affect desulfurization depth and desulfuration efficiency, cause desulfurization It is unqualified.
System processing using the steady salt of heat in the removing organic amine liquid of the utility model contains the organic amine liquid of the steady salt of heat Method, can by organic amine liquid to be processed strong cation and the steady salt anionic of heat remove (such as sodium ion and acetic acid simultaneously Radical ion removes simultaneously will form sodium acetate), and accumulate in demineralized water and emitted to a certain concentration.
According to the utility model, the organic amine liquid, demineralized water and electrode solution enter before the membrane stack 4 by heat exchange Reason, the temperature through treated the organic amine liquid, demineralized water and electrode solution of exchanging heat are 5-35 DEG C, preferably 15-25 DEG C.
According to the utility model, the organic amine liquid, demineralized water and electrode solution enter before the membrane stack 4 by filtering Reason, with the solid particulate matter for removing organic amine liquid, partial size is 0.1-1 microns in demineralized water and electrode solution.
According to the utility model, under preferable case, in the organic amine liquid treatment process, the organic amine liquid and described The flow of demineralized water can be 1-10m3/ h, preferably 2-5m3/ h, the flow of the electrode solution can be 1-5m3/ h, preferably 2-4m3/h.The organic amine liquid, demineralized water and electrode solution are divided into multiply tributary before entering the membrane stack 4, respectively enter The flow of respective compartment in membrane stack 4, each stock tributary is constant, or is equally assigned into identical flow.
The utility model will be described in detail by embodiment below.
Embodiment 1
The system of the steady salt of heat is skid-mounted system, structural schematic diagram such as Fig. 1 in removing organic amine liquid provided in this embodiment Shown, which includes: organic amine liquid storage device 1, electrode solution storage device 2, desalination water storage apparatus 3, membrane stack 4 and control Maincenter 5, wherein the membrane stack 4 is respectively communicated with the organic amine liquid storage device 1, the electrode solution storage device 2 and described removes Salt water storage apparatus 3；The membrane stack 4 is provided at least one organic amine liquid import, the outlet of organic amine liquid, waste liquid import, waste liquid Outlet, electrode solution import and electrode solution outlet；First is respectively arranged at organic amine liquid exit and the waste liquid outlet Conductivity meter 91 and the second conductivity meter 92, for monitoring the liquid electric at organic amine liquid exit and the waste liquid outlet Conductance；First is provided on organic amine liquid exit to the Location Detection of Medium Transportation Pipeline between the organic amine liquid storage device 1 Regulating valve 61 is provided with the second tune on the desalination water storage apparatus 3 to the Location Detection of Medium Transportation Pipeline between the waste liquid entrance Save valve 62；The system also includes control axis 5, come from first conductivity meter 91 and/or the second conductivity for receiving The conductivity signal of instrument 92, and adjusted according to the conductivity signal of first conductivity meter 91 and/or the second conductivity meter 92 The aperture of first regulating valve 61 and/or second regulating valve 62.
The membrane stack 4 includes being oppositely arranged on the anode plate, cathode plate and setting at 4 both ends of membrane stack in the anode plate and yin The mould group containing multiple amberplexes between pole plate；Region between the anode plate and the mould group forms anode chamber I- 1, the region between the cathode plate and the mould group forms cathode chamber I-2；The multiple amberplex is in the mould group It is separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately；The ion of two adjacent amberplexes selects Permeability is different；The organic amine liquid import and the outlet of organic amine liquid are set in the heteropleural of each amine liquid chamber II, each The waste liquid import and waste liquid outlet is arranged in the heteropleural of the waste liquid chamber III, in the different of the anode chamber I-1 and cathode chamber I-2 The electrode solution liquid outlet and electrode solution outlet is respectively set in side；The liquid outlet and the film of the organic amine liquid storage device 1 The organic amine liquid inlet communication of the amine liquid chamber II of heap 4 is arranged, the inlet and the membrane stack 4 of the organic amine liquid storage device 1 Amine liquid chamber II organic amine liquid outlet setting, formed closed circuit, become organic amine liquid circulation loop；The electrode solution The electrode solution inlet communication of the electrode solution liquid outlet of storage device 2 and the anode chamber I-1 and cathode chamber I-2 are arranged, the electricity The electrode solution outlet of the electrode solution inlet of pole liquid storage device 2 and the anode chamber I-1 and cathode chamber I-2 are arranged, shape At closed circuit, become electrode solution circulation loop；The demineralized water liquid outlet of the desalination water storage apparatus 3 and the waste liquid chamber The waste liquid inlet communication of III is arranged, the waste liquid of the demineralized water inlet of the desalination water storage apparatus 3 and the waste liquid chamber III Outlet setting, forms closed circuit, becomes desalination water-flow circuit.
Organic amine liquid export pipeline is also connected in the organic amine liquid circulation loop, for the organic of hot steady salt will to be removed Amine liquid is exported to the organic amine liquid reclaiming system of the steady salt of removing heat, is provided with third regulating valve 63 on the amine liquid export pipeline, Waste liquid outlet pipeline is also connected on the desalination water storage apparatus 3, for by outside discharging of waste liquid to the system, the waste liquid The 4th regulating valve 64 is provided on outlet pipeline, the control axis 5 is also used to receive from 91 He of the first conductivity meter The conductivity signal of second conductivity meter 92, and believed according to the conductivity of first conductivity meter 91 and the second conductivity meter 92 Number adjust the aperture of the third regulating valve 63 and the 4th regulating valve 64.
First circulation pump 71 is provided in the organic amine liquid circulation loop, the electrode solution circulation loop is provided with second Circulating pump 72 is provided with third circulating pump 73 in the desalination water-flow circuit, is respectively used to store the organic amine liquid and fills The amine liquid chamber II that the Matter Transfer in 1 is pumped into membrane stack 4 is set, the Matter Transfer in electrode solution storage device 2 is pumped into the sun of membrane stack 4 Pole room I-1 and cathode chamber I-2, the Matter Transfer in desalination water storage apparatus 3 is pumped into the waste liquid chamber III of membrane stack 4.Described One circulating pump 71, second circulation pump 72 and third circulating pump 73 in is additionally provided with frequency converter, for control each pump switch and Pump speed.The first circulation pump 71, second circulation pump 72 are identical with the starting speed of third circulating pump 73 and normal from starting to The time of operating is 35s, and first circulation pump 71, second circulation pump 72 and third circulating pump 73 are from running well to thorough The time of stopping is identical, is 5s.
In the connecting pipeline of the respective compartment of each circulating pump to membrane stack 4, it is additionally provided with filter, the filter is Filter cartridge type filter, filtration core are that pp cotton folds cotton core, and filtering accuracy is 0.1 micron.
The filter outlet is additionally provided with differential manometer, supervises to the retention state in the filter core gap of the filter Control.
In the connecting pipeline of the respective compartment in each circulating pump to membrane stack 4, it is additionally provided with flowmeter, the flow Cutout detection device is provided on meter.
The import of organic amine liquid, waste liquid import and the electrode solution entrance of the membrane stack 4 are respectively arranged with heat exchanger and temperature Meter regulates and controls the temperature for entering the material of the membrane stack 4 to 20 DEG C.
The system is additionally provided with nitrogen gas generating device, and the feed-line of the nitrogen gas generating device is respectively connected to described organic Amine liquid storage device 1, electrode solution storage device 2 and desalination water storage apparatus 3 carry out the storage device in each circulation loop Nitrogen envelope, it is ensured that amine liquid etc. completely cuts off air in respective circulating tank, will not be oxidized.
It is additionally provided with cleaning device in the membrane stack 4, to the first amberplex A and/or the second amberplex B It is cleaned.
Organic amine liquid tank gage 81 is additionally provided on the organic amine liquid storage device 1, on the desalination water storage apparatus 2 It is additionally provided with demineralized water tank gage 82, is respectively used to detect the organic amine liquid storage device 1 and the desalination water storage apparatus 2 Then the liquid level signal of the two is sent to the control axis 5 by interior liquid level, the control axis 5 is according to the organic amine The liquid level signal of liquid tank gage 81 and/or demineralized water tank gage 82 adjusts the 5th regulating valve 65 on the amine liquid intake pipeline And/or the aperture of the 6th regulating valve 66 on the demineralized water intake pipeline, and then control the organic amine liquid storage device 1 And/or the dosage and flow velocity of the fluid infusion of the desalination water storage apparatus 2；The control axis 5 can also be according to the organic amine The liquid level signal of liquid tank gage 81 and/or demineralized water tank gage 82 further controls the third regulating valve 63 and/or the 4th and adjusts Aperture and the switch opportunity of valve 64 are saved, the organic amine liquid and/or demineralized water in Collaborative Control organic amine liquid circulation loop are recycled back to The loop start of waste liquid or stopping and circular flow in road.
It, will be wait locate when using the system processing of the steady salt of heat in removing organic amine liquid above-mentioned containing the organic amine liquid of the steady salt of heat Reason organic amine liquid is introduced the organic amine liquid storage device 1 of the system by external pipeline, and demineralized water is introduced to the system In desalination water storage apparatus 3, it will be passed through electrode solution in electrode solution storage device 2, organic amine liquid circulation is then pumped into institute Desalination water-circulating pump in the desalination water storage apparatus 3, is entered the waste liquid chamber of the membrane stack 4 by the amine liquid chamber II for stating membrane stack 4 Electrode solution in electrode solution storage device 2 is recycled the anode chamber I-1 and cathode chamber I-2 for being pumped into the membrane stack 4 by III respectively；It will The anode plate and cathode plate of the membrane stack 4 are connect with the anode and cathode of flame proof DC power supply respectively, and circulation is made to be pumped into the film The organic amine liquid to be processed of heap 4 carries out the steady salt removing of heat and handles, and obtains the organic amine liquid of the steady salt of removing heat and is enriched with the steady salt of heat Demineralized water, the organic amine liquid of the steady salt of removing heat to be obtained and the demineralized water of the steady salt of enrichment heat meet recycling and discharge standard respectively When, the organic amine liquid of the steady salt of removing heat obtained after processing is delivered to organic amine liquid reclaiming system, the richness that will be obtained after processing The demineralized water of the steady salt of thermal-arrest as discharging of waste liquid to the system outside.
In the present embodiment, organic amine liquid to be processed is derived from petrochemical industry Co., Ltd, Dalian Western Pacific, composition such as table 1 Shown, the membrane stack 4 is yin-yang membrane stack, structural schematic diagram and working principle as shown in Figure 1, the first amberplex A For cation-exchange membrane, it includes periodically alternately in the yin-yang membrane stack that the second amberplex B, which is anion-exchange membrane, The 100 groups of cation-exchange membranes and anion-exchange membrane of arrangement, from anode plate to cathode plate direction, the mould group successively includes being in The multiple anion-exchange membrane B and cation-exchange membrane A, each anion-exchange membrane B and cation being periodically arranged alternately are handed over It changes film A and forms repetitive unit, the repetitive unit that multiple groups amberplex is formed, which is separated out, multiple to be periodically arranged alternately Amine liquid chamber II and waste liquid chamber III.Demineralized water is deionized water, and the electrode solution is the metabisulfite solution that concentration is 6 weight %.Institute It states and is provided with frequency converter in first circulation pump 71, second circulation pump 72 and third circulating pump 73, frequency converter setting frequency is 29Hz, the circular flow for controlling organic amine liquid and demineralized water is 4m3The flow that pumps out of/h, electrode solution are 2m3/ h flows into anode chamber The tributary flow of I-1 and cathode chamber I-2 is 1m3/ h, the voltage of the flame proof DC power supply are 130V, electric current 110A, electricity Current density is 150mA/cm2, the control axis 5 sets the conductivity signal difference of the organic amine liquid as 10ms, demineralized water Conductivity signal value as discharging of waste liquid is 55ms, when the conductivity signal difference that first conductivity meter 91 measures is When 10ms, the control axis 5 regulates and controls first regulating valve 61 and closes, and opens and be arranged on the export pipeline of organic amine liquid Third regulating valve 63, treated that organic amine liquid is exported to organic amine liquid reclaiming system by up to standard, when second conductivity When the amine liquid conductivity signal value that instrument 92 measures is 55ms, the control axis 5 regulates and controls second regulating valve 62 and closes, and opens The 4th regulating valve 64 being arranged on waste liquid outlet pipeline is opened, using the demineralized water of the steady salt of enrichment heat as waste liquid discharge system.
The organic amine liquid that takes that treated and demineralized water are detected, and testing result is as shown in table 1.
Table 1
Sample Organic amine liquid concentration Conductivity Na+Concentration Cl-Concentration The steady salinity of heat
Organic amine liquid to be processed 25.5 weight % 14ms 8300mg/L 15240mg/L 6.69 weight %
Organic amine liquid after processing 26.19 weight % 4ms 600mg/L 1160mg/L 0.75 weight %
Demineralized water - 55ms 16600mg/L 31640mg/L 12.87 weight %
From table 1 it follows that the conductivity of organic amine liquid reduces after processing, sodium ion, chloride ion and the steady salinity of heat Decline, and demineralized water is that 0 (deionized water) is increased to 55ms by conductivity, the steady salinity of heat reaches 12.87 weight %, illustrate to It handles the steady salt of the heat in organic amine liquid to enter in demineralized water under the action of DC electric field, is enriched the demineralized water conduct of hot steady salt Discharging of waste liquid has achieved the purpose that the steady salt removing of heat in organic amine liquid.
Embodiment 2
In removing organic amine liquid provided in this embodiment the system of the steady salt of heat and using heat in the removing organic amine liquid surely The method such as embodiment 1 of organic amine liquid of the system processing of salt containing the steady salt of heat, unlike, the membrane stack 4 is bipolar membrane stack, Its structural schematic diagram and working principle are as shown in Fig. 2, the first amberplex A is Bipolar Membrane, second ion exchange Film B is anion-exchange membrane, includes 100 groups of Bipolar Membranes being periodically arranged alternately and anion-exchange membrane in the bipolar membrane stack And third amberplex C, the third amberplex C are cation-exchange membrane, are set by the close anode plate, From third amberplex C to cathode plate direction, the mould group successively includes handing in the multiple anion being periodically arranged alternately It changes film B and Bipolar Membrane A, each anion-exchange membrane B and Bipolar Membrane A forms a repetitive unit, multiple groups amberplex is formed Repetitive unit be separated out multiple amine liquid chamber II and waste liquid chamber III being periodically arranged alternately.The control axis 5 sets described The conductivity signal difference of organic amine liquid is 15ms, and demineralized water is 55ms as the conductivity signal value of discharging of waste liquid, when described When the conductivity signal difference that first conductivity meter 91 measures is 15ms, the control axis 5 regulates and controls first regulating valve 61 It closes, and opens the third regulating valve 63 being arranged on the export pipeline of organic amine liquid, treated that organic amine liquid is defeated by up to standard It is described when the amine liquid conductivity signal value that second conductivity meter 92 measures is 55ms out to organic amine liquid reclaiming system Control axis 5 regulates and controls second regulating valve 62 and closes, and opens the 4th regulating valve 64 being arranged on waste liquid outlet pipeline, will be rich The demineralized water of the steady salt of thermal-arrest is as waste liquid discharge system.
Organic amine liquid to be processed is technical pure MDEA autogamy (hydrochloric acid is added in amine liquid) organic amine liquid, composition such as table 2 Shown, the organic amine liquid that takes that treated and demineralized water are detected, and testing result is as shown in table 2.
Table 2
Sample Organic amine liquid concentration Conductivity Metal cation concentration Cl-Concentration
Organic amine liquid to be processed 25 weight % 18.8ms 0mg/L 20000mg/L
Organic amine liquid after processing 25 weight % 3.8ms 0mg/L 800mg/L
Demineralized water - 55ms 0mg/L 35870mg/L
From Table 2, it can be seen that processing after organic amine liquid conductivity reduce, chlorine ion concentration decline, and demineralized water by Conductivity is that 0 (deionized water) is increased to 55ms, and main component is hydrochloric acid in demineralized water, and wherein chloride ion content is 35870mg/ L illustrates under the action of Bipolar Membrane, the H that the chloride ion in organic amine liquid to be processed and Bipolar Membrane generate+It is combined into demineralized water Storage device, formation hydrochloric acid, and the OH that Bipolar Membrane generates-Into in organic amine liquid circulation loop, make in organic amine liquid to be processed The hydrochloric acid of addition is neutralized, to reach the removing purpose of the steady salt of heat in organic amine liquid to be processed.
Embodiment 3
In removing organic amine liquid provided in this embodiment the system of the steady salt of heat and using heat in the removing organic amine liquid surely The method such as embodiment 1 of organic amine liquid of the system processing of salt containing the steady salt of heat, unlike, it is defeated which is additionally provided with lye Enter device, the organic amine liquid inlet communication setting of the liquid outlet of the lye input unit and the membrane stack 4.The lye is hydrogen Sodium oxide molybdena, the concentration of the lye are 30 weight %.
Organic amine liquid to be processed is technical pure MDEA autogamy (hydrochloric acid is added in amine liquid) organic amine liquid, composition such as table 3 Shown, the organic amine liquid that takes that treated and demineralized water are detected, and testing result is as shown in table 3.
Table 3
From table 3 it is observed that the conductivity of organic amine liquid reduces after processing, sodium ion, chloride ion and the steady salinity of heat Decline, and demineralized water by conductivity be 0 (deionized water) be increased to 55ms, illustrate work as organic amine liquid to be processed in without metal sun from The period of the day from 11 p.m. to 1 a.m, can method by adding lye, that is, the removing that yin-yang membrane stack carries out the steady salt of heat to organic amine liquid to be processed can be used Processing, reach with the identical desalting effect of the organic amine liquid containing metal cation, and treated that organic amine liquid will not be made At the loss of organic amine liquid.
Embodiment 4
In removing organic amine liquid provided in this embodiment the system of the steady salt of heat and using heat in the removing organic amine liquid surely The method such as embodiment 1 of organic amine liquid of the system processing of salt containing the steady salt of heat, except that in the yin-yang membrane stack used, amine The hydrogen-oxygen type strong-base anion-exchange resin and sodium form cation exchange resin that dosage volume ratio is 1:1 are packed full in liquid chamber II Mixture.
The control axis 5 sets the conductivity signal value of the organic amine liquid discharge as 0ms, and demineralized water is arranged as waste liquid The conductivity signal value put is 55ms, described when the amine liquid conductivity signal value that first conductivity meter 91 measures is 0ms Control axis 5 regulates and controls first regulating valve 61 and closes, and opens the third regulating valve being arranged on the export pipeline of organic amine liquid 63, treated that organic amine liquid is exported to organic amine liquid reclaiming system by up to standard, measures when second conductivity meter 92 When amine liquid conductivity signal value is 55ms, the control axis 5 regulates and controls second regulating valve 62 and closes, and opens waste liquid outlet The 4th regulating valve 64 being arranged on pipeline, using the demineralized water of the steady salt of enrichment heat as waste liquid discharge system.
The organic amine liquid that takes that treated and waste liquid are detected, and testing result is as shown in table 4.
Table 4
Sample Organic amine liquid concentration Conductivity Na+Concentration Cl-Concentration The steady salinity of heat
Organic amine liquid to be processed 25.5 weight % 14ms 8300mg/L 15240mg/L 6.69 weight %
Organic amine liquid after processing 26.3 weight % 0ms <10mg/L <10mg/L 0 weight %
Demineralized water - 55ms 16880mg/L 32100mg/L 13.1 weight %
As can be seen from Table 4, in ion exchange resin as under conducting medium effect, electrodialysis desalination depth is improved, Under identical treatment conditions, sodium ion, chloride ion and the steady salinity of heat are dropped to close to 0 in organic amine liquid after processing, and are removed Salt water is that 0 (deionized water) is increased to 55ms by conductivity, and the steady salinity of heat reaches 13.1 weight %, illustrates organic amine to be processed Steady salt almost all under the action of DC electric field of heat in liquid enters in demineralized water, is enriched the demineralized water of hot steady salt as useless Liquid discharge has achieved the purpose that the steady salt of heat is removed in depth in organic amine liquid.
Embodiment 5
In removing organic amine liquid provided in this embodiment the system of the steady salt of heat and using heat in the removing organic amine liquid surely The method such as embodiment 2 of organic amine liquid of the system processing of salt containing the steady salt of heat, except that in the bipolar membrane stack used, amine Hydrogen-oxygen type strong-base anion-exchange resin is packed full in liquid chamber II.
The control axis 5 sets the conductivity signal value of the organic amine liquid discharge as 0ms, and demineralized water is arranged as waste liquid The conductivity signal value put is 55ms, described when the amine liquid conductivity signal value that first conductivity meter 91 measures is 0ms Control axis 5 regulates and controls first regulating valve 61 and closes, and opens the third regulating valve being arranged on the export pipeline of organic amine liquid 63, treated that organic amine liquid is exported to organic amine liquid reclaiming system by up to standard, measures when second conductivity meter 92 When amine liquid conductivity signal value is 55ms, the control axis 5 regulates and controls second regulating valve 62 and closes, and opens waste liquid outlet The 4th regulating valve 64 being arranged on pipeline, using the demineralized water of the steady salt of enrichment heat as waste liquid discharge system.
The organic amine liquid that takes that treated and demineralized water are detected, and testing result is as shown in table 5.
Table 5
Sample Organic amine liquid concentration Conductivity Metal cation concentration Cl-Concentration
Organic amine liquid to be processed 25 weight % 18.8ms 0mg/L 20000mg/L
Organic amine liquid after processing 25 weight % 0ms 0mg/L <10mg/L
Demineralized water - 55ms 0mg/L 35590mg/L
As can be seen from Table 5, in ion exchange resin as under conducting medium effect, electrodialysis desalination depth is improved, Under identical treatment conditions, chlorine ion concentration is dropped to close to 0 in organic amine liquid after processing, and demineralized water is 0 by conductivity (deionized water) is increased to 55ms, illustrate the steady salt of heat in organic amine liquid to be processed under the action of DC electric field almost all into Enter in demineralized water, be enriched the demineralized water of hot steady salt as discharging of waste liquid, has reached what the steady salt of heat in organic amine liquid was removed in depth Purpose.
The system that can be seen that the steady salt of heat in removing organic amine liquid provided by the utility model by the result of table 1-5 is suitable Organic amine liquid of the processing containing the steady salt of different heat is closed, high degree of automation, desalting ability is strong, and whole process is not necessarily to manual intervention, saves Human cost.Organic amine liquid containing the steady salt of heat is handled using the system, the same of zwitterion in amine liquid not only may be implemented Step removing, moreover it is possible to which the solid particulate matter effectively in removing organic amine liquid greatly reduces the consumption of lye, and waste liquid discharging amount is low, increases The reusable service life of strong organic amine liquid.
Preferred embodiments of the present invention are described in detail above, still, the utility model is not limited to this.At this In the range of the technology design of utility model, a variety of simple variants can be carried out to the technical solution of the utility model, including each Technical characteristic is combined with any other suitable method, these simple variants and combination equally should be considered as the utility model Disclosure of that belongs to the protection scope of the utility model.

Claims (11)

1. the system of the steady salt of heat in a kind of removing organic amine liquid, which includes: that organic amine liquid storage device (1), electrode solution are deposited Storage device (2), desalination water storage apparatus (3), membrane stack (4) and control axis (5), which is characterized in that the membrane stack (4) connects respectively Lead to the organic amine liquid storage device (1), the electrode solution storage device (2) and the desalination water storage apparatus (3)；The film Heap (4) is provided at least one organic amine liquid import, the outlet of organic amine liquid, waste liquid import, waste liquid outlet, electrode solution import and electricity The outlet of pole liquid；The first conductivity meter (91) and the second electricity are respectively arranged at organic amine liquid exit and the waste liquid outlet Electrical conductivity instrument (92), for monitoring the liquid electric conductivity at organic amine liquid exit and the waste liquid outlet；The organic amine The first regulating valve (61), institute are provided on liquid exit to the Location Detection of Medium Transportation Pipeline between the organic amine liquid storage device (1) It states and is provided with the second regulating valve (62) on the Location Detection of Medium Transportation Pipeline between desalination water storage apparatus (3) to the waste liquid entrance； The control axis (5) is used to receive the conductivity from first conductivity meter (91) and/or the second conductivity meter (92) Signal, and described first is adjusted according to the conductivity signal of first conductivity meter (91) and/or the second conductivity meter (92) The aperture of regulating valve (61) and/or second regulating valve (62).
2. system according to claim 1, wherein the membrane stack (4) includes the anode for being oppositely arranged on membrane stack (4) both ends Plate, cathode plate and the mould group containing multiple amberplexes being arranged between the anode plate and cathode plate；The anode plate Region between the mould group forms anode chamber (I-1), and the region between the cathode plate and the mould group forms cathode chamber (I-2)；The multiple amberplex is separated out multiple amine liquid chambers (II) being periodically arranged alternately and is given up in the mould group Liquid chamber (III)；The ion-selective permeability of two adjacent amberplexes is different；In the heteropleural of each amine liquid chamber (II) The organic amine liquid import and the outlet of organic amine liquid are set, the heteropleural of each waste liquid chamber (III) be arranged the waste liquid into Mouth and waste liquid outlet, are respectively set the electrode solution import and electrode in the heteropleural of the anode chamber (I-1) and cathode chamber (I-2) Liquid outlet；
The organic amine liquid storage device (1) is provided with inlet and liquid outlet, the liquid outlet and the organic amine liquid import Connection, the inlet and the organic amine liquid outlet form organic amine liquid circulation loop；
The electrode solution storage device (2) is provided with electrode solution inlet and electrode solution liquid outlet, the electrode solution liquid outlet with The electrode solution inlet communication, the electrode solution inlet and the electrode solution outlet form electrode solution circulation loop；
The desalination water storage apparatus (3) is provided with demineralized water inlet and demineralized water liquid outlet, the demineralized water liquid outlet with The waste liquid inlet communication, the demineralized water inlet are connected to the waste liquid outlet, form desalination water-flow circuit.
3. system according to claim 2, wherein each of be separated out the amine liquid chamber (II) in the membrane stack (4) Filling ion-exchange resin is gone back between two amberplexes；The ion exchange resin is strongly acidic cation exchange tree Rouge and/or strong-base anion-exchange resin.
4. system according to claim 2, wherein the membrane stack (4) is yin-yang membrane stack or bipolar membrane stack, the membrane stack (4) the different amberplex of two adjacent selective penetrated properties includes the first amberplex (A) and the second ion exchange in Film (B)；
When the membrane stack (4) are yin-yang membrane stack, first amberplex (A) and the second amberplex (B) are respectively Anion-exchange membrane or cation-exchange membrane；When the membrane stack (4) be bipolar membrane stack when, first amberplex (A) and Second amberplex (B) is respectively anion-exchange membrane or Bipolar Membrane.
5. the system according to any one of claim 2-4, wherein be also connected in the organic amine liquid circulation loop Organic amine liquid export pipeline, for exporting the organic amine liquid of the steady salt of removing heat to organic amine liquid reclaiming system, the organic amine It is provided on liquid export pipeline third regulating valve (63), waste liquid outlet pipeline is also connected in the desalination water-flow circuit, used In by outside discharging of waste liquid to the system, the 4th regulating valve (64), the control axis are provided on the waste liquid outlet pipeline (5) it is also used to receive the conductivity signal from first conductivity meter (91) and/or the second conductivity meter (92), and according to The conductivity signal of first conductivity meter (91) and/or the second conductivity meter (92) adjusts the third regulating valve (63) And/or the aperture of the 4th regulating valve (64).
6. the system according to any one of claim 2-4, wherein be provided in the organic amine liquid circulation loop One circulating pump (71), the electrode solution circulation loop are provided with second circulation pump (72), are arranged in the desalination water-flow circuit There are third circulating pump (73), is respectively used to for the Matter Transfer in the organic amine liquid storage device (1) to be pumped into the amine of membrane stack (4) Matter Transfer in electrode solution storage device (2) is pumped into anode chamber (I-1) and the cathode chamber (I- of membrane stack (4) by liquid chamber (II) 2), the Matter Transfer in desalination water storage apparatus (3) is pumped into the waste liquid chamber (III) of membrane stack (4).
7. system according to claim 6, wherein in the connecting pipeline of the respective compartment of each circulating pump to membrane stack (4) On, it is additionally provided with filter.
8. system according to claim 7, wherein the filter is filter cartridge type filter, and filtering accuracy is that 0.1-1 is micro- Rice.
9. the system according to any one of claim 2-4, wherein the organic amine liquid import of the membrane stack (4), waste liquid Import and electrode solution entrance are respectively arranged with heat exchanger and thermometer, the temperature of the material for regulating and controlling to enter the membrane stack (4) Degree.
10. the system according to any one of claim 2-4, wherein the system is additionally provided with lye input unit, institute The feed-line for stating lye input unit accesses the organic amine liquid storage device (1).
11. the system according to any one of claim 2-4, wherein the system is additionally provided with inert gas access dress It sets, the feed-line of the inert gas access device is respectively connected to organic amine liquid storage device (1), electrode solution storage device (2) and desalination water storage apparatus (3).
CN201821123830.3U 2018-07-16 2018-07-16 The system for removing the steady salt of heat in organic amine liquid Active CN208786104U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201821123830.3U CN208786104U (en) 2018-07-16 2018-07-16 The system for removing the steady salt of heat in organic amine liquid

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201821123830.3U CN208786104U (en) 2018-07-16 2018-07-16 The system for removing the steady salt of heat in organic amine liquid

Publications (1)

Publication Number Publication Date
CN208786104U true CN208786104U (en) 2019-04-26

Family

ID=66202460

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201821123830.3U Active CN208786104U (en) 2018-07-16 2018-07-16 The system for removing the steady salt of heat in organic amine liquid

Country Status (1)

Country Link
CN (1) CN208786104U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112439321A (en) * 2019-08-29 2021-03-05 大禹环服（北京）科技有限公司 Electrodialysis method for removing heat-stable amine salt

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112439321A (en) * 2019-08-29 2021-03-05 大禹环服（北京）科技有限公司 Electrodialysis method for removing heat-stable amine salt

Similar Documents

Publication Publication Date Title
CN108970334A (en) Regenerative system and application thereof for rich carbon amine liquid
CN107089753B (en) The processing method of power plant desulfurization wastewater
CN110721553A (en) System and method for removing heat stable salt in organic amine liquid
CN109607705B (en) Industrial water dechlorination method
CN113101808B (en) CO (carbon monoxide) 2 Electrodialysis regeneration device and method for trapping amine liquid
CN109809964A (en) A method of neopentyl glycol is purified using bipolar membrane electrodialysis system
CN208786104U (en) The system for removing the steady salt of heat in organic amine liquid
CN201148367Y (en) Electric softening installation
KR20130077164A (en) Water treatment apparatus for fuel cell
CN208082235U (en) The desalter of electrodialysis coupled ion exchanger resin
CN113457451A (en) Method for regenerating carbon capture absorbent morpholine by bipolar membrane electrodialysis
CN103406025A (en) Technology for continuously removing heat steady salts from alcohol amine desulfurization solution by using double-membrane reactor-magnetic electrodialysis method
KR20190079851A (en) Electrodeionization with excellent boron removal efficiency
JP3966103B2 (en) Operation method of electrodeionization equipment
CN209974381U (en) Dechlorination machine
JP2011121027A (en) Electric type deionized water producing apparatus
JP4662277B2 (en) Electrodeionization equipment
CN108392957A (en) A kind of flue gas desulphurization system
CN212269765U (en) Concentrated decrement device of power plant&#39;s desulfurization waste water
CN2839253Y (en) Rolling electric desalting device with variable resin filling ratio
CN213771442U (en) Electrodialysis and bipolar membrane electrodialysis coupled degraded amine liquid purification and recovery device
JP7146568B2 (en) Organic solvent purification method and purification apparatus
Korngold Electrodialysis unit: Optimization and calculation of energy requirement
CN220294443U (en) Device for removing heat stable salt through amine liquid electrodialysis
CN116236907A (en) Thioglycollic acid preparation method based on bipolar membrane electrodialysis method

Legal Events

Date Code Title Description
GR01 Patent grant
GR01 Patent grant