CN101054532A - Method and device for rotational flow alkali removing - Google Patents
Method and device for rotational flow alkali removing Download PDFInfo
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- CN101054532A CN101054532A CN 200610025675 CN200610025675A CN101054532A CN 101054532 A CN101054532 A CN 101054532A CN 200610025675 CN200610025675 CN 200610025675 CN 200610025675 A CN200610025675 A CN 200610025675A CN 101054532 A CN101054532 A CN 101054532A
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Abstract
The invention provides a method for spiral flow dealkalization, comprising the steps of (a) obtaining a mixture containing water of 10000mg/L-50000mg/L by reaction between 95-99.9vol% C3-C5 alkane containing water-soluble alkaline impurities and 0.1-5.0 vol% alkaline removed water at 20-120 degree under 0.01MPa-0.50MPa and (b) obtaining a dealkalized alkane by centrifugal rotation and separating the mixture obtained in step (a). The dealkalization method of C3-C5 alkane in the invention is capable of apparently prolonging the service life of C3-C5 dealkalization catalyst.
Description
Technical field
The invention belongs to liquid/liquid separation technology field, be specifically related to slough C
3～C
5The method of the water-soluble alkaline impurity in the alkane.
Background technology
At petroleum chemical industry, the carbon three, butane, the C 5 alkane that obtain through the gas fraction device then carry out subsequent reactions such as etherificate.Above-mentioned carbon three alkane, butane, C 5 alkane are through taking off H
2S and mercaptan, remaining alkali lye material in the system is as amine, alkali, alkalimetal ion, acetonitrile, propionitrile and nitride.These alkaline matters will cause an acidic catalyst in the follow-up etherification reaction process to be poisoned, and shorten the work-ing life of catalyzer, the steady running cycle of having reduced whole device.
For fear of above-mentioned poisoning problem, at present, at C
3～C
5Extensively adopt gravity settler and coalescer to remove C in desulfurization and the desulfurization ether process
3～C
5Droplets entrained or droplet also have the water washing of employing C
3～C
5The method of middle alkali lye.
Use gravity settler to realize C
3～C
5The isolating weak point of alkane and alkali lye drop, gasoline and alkali lye is that equipment volume is bigger, and the consumption of metallic substance is also bigger, and cost is also than higher, and the dealkalize precision is not high yet.In addition, at sweetening agent foaming, " race sweetening agent " when operating mode occurs, C
3～C
5The foam sweetening agent that alkane carries, conventional slurry tank are can't be isolating.
And use the weak point of coalescer to be, and go back the general standard of none so far for the design of the size of coalescer, there is not a kind of accurate method can determine that the filter core of coalescer under given flow needs great filtration capacity actually.The filter size that different manufacturerss provides is completely different.In addition, also insufficient to the filtration capacity of strainer with the research of the relation that is filtered material, easily cause the blocked shortcoming of element when existing liquid unholiness.Some strainer puts into operation, does not cross several hrs and the high pressure drop that is difficult to accept will occur.This shows, design and produce and satisfy the amine liquid coalescer production application request, that can long period stabilize the economy operation suitable difficulty is arranged.
In addition, washing dealkalize system commonly used generally could adopt water wash system to the amine liquid concentration of system greater than 50% system.The equipment of water wash system has mixing tank, settling vessel and washing pump etc., also needs the make up water wash water, and certain material consumption and energy consumption are arranged.
In sum, all there is weak point at present common solution MTBE device (the methyl tertiary butyl ether makeup is put), gasoline etherification device butane, the gasoline technique means of carrying alkaline matter secretly.Topmost, the alkali lye that settlement separate still coarse separation all can't solve raw material under the amine liquid foaming operating mode when carrying a large amount of spumescence solvent secretly is deviate from alkali lye to reclaim.Secondly, the spent resource of several schemes is all many, is difficult to the ensuring equipment long-term operation.Simple settlement separate required equipment volume is bigger, floor space is bigger, be difficult to use in the transformation of the device that builds up compact in design, the price of coalescent filter core own is just relatively more expensive, and age limit is arranged, thereby the cycle of operation is short, the operation anaphase effect is poor, must install two groups, regularly clean and change; The running cost of water wash system scheme itself is just than higher, and suitability is also limited.Thereby it is better that we need seek suitability, more stable, isolation technique means efficiently.
Also some available technology adopting are arranged the rotational flow alkali removing method liquid of the present invention-liquid mixture system is separated, but be not suitable for being used for separating C of the present invention
3～C
5Alkane.Reason is C
3～C
5Boiling point of alkanes is low, gasification and loss is carried a large amount of spumescence solvents secretly also easilier easily, thus brought great difficulty to separation.And stop up through regular meeting in the cyclonic separation equipment, can't steady running, or have the impurity salt to separate out, cause system's instability.
In a word, because the shortcoming that prior art exists, so still unresolved up to now C
3～C
5The problem of dealkalize far can not satisfy the expectation of catalyzer long-term operation in alkane ether-based device such as the MTBE device.Therefore, this area presses for a kind of improved C of exploitation
3～C
5Dealkalization method and device, thereby the process that advances MTBE device catalyzer long period to use widely.
Summary of the invention
The objective of the invention is: overcome the above-mentioned defective of prior art, a kind of improved C is provided
3～C
5The dealkalization method of alkane, thus C prolonged
3～C
5The process that dealkalize catalyzer long period is used.
First aspect present invention provides a kind of method of rotational flow alkali removing, may further comprise the steps: (a) C that contains water-soluble alkaline impurity of 95～99.9 parts by volume
3～C
5The dealkalize water of alkane and 0.1～5.0 parts by volume is at 20～120 ℃, 0.01MPa～0.50MPa mixes down, obtaining water content is 10000mg/L～50000mg/L mixture, wherein said water-soluble alkaline impurity accounts for 1～30wt% of alkane weight, (b) the centrifugal rotation of mixture that obtains of step (a) separates, and obtains the alkane of dealkalize.
In a preferred embodiment, the mixture water content in the step (a) is 10000mg/L～15000mg/L.
In a preferred embodiment, the described water-soluble alkaline impurity in the step (a) accounts for 15～25wt% of alkane weight.
In a preferred embodiment, the mixing step of step (a) carries out under 0.05MPa～0.25MPa.
In a preferred embodiment, described water-soluble alkaline impurity is amine, alkali, alkalimetal ion, acetonitrile, propionitrile, nitride and combination thereof.
In a preferred embodiment, described dealkalize water is de-mineralized water, de-oxygenised water or condensed water.
In a preferred embodiment, it is after the drop of 20 μ m～50 μ m that the described dealkalize water of step (a) forms median size earlier, mixes with described alkane again.
In a preferred embodiment, at 10～100 ℃, under 0.05MPa～0.25MPa, each self-forming median size of described dealkalize water and alkane is the drop of 20 μ m～50 μ m, mixes then.
The rotational flow alkali removing device that another aspect of the present invention provides a kind of method according to claim 1 to adopt, described tripping device comprises water injection equipment, liquid-liquid mixer and cyclone separator, described water injection equipment is located at the upstream of described liquid-liquid mixer, and described swirler separator is located at the downstream of described liquid-liquid mixer.
In a preferred embodiment, described liquid-liquid mixer is a static mixer.
In a preferred embodiment, the downstream of described cyclone separator also is provided with waste disposal plant.
In a preferred embodiment, described cyclone separator pressure is reduced to 0.05MPa～0.25MPa.
In a preferred embodiment, between liquid-liquid mixer and cyclone separator, also be provided with settling vessel.
The present invention has an aspect that a kind of MTBE ether-based device is provided again, wherein the described rotational flow alkali removing device of the with good grounds claim 5 of the provided upstream of MTBE methyltertiarvbutyl ether reactor.
A further aspect of the invention provides a kind of rotational flow alkali removing method or rotational flow alkali removing device at C
3～C
5Alkane carries out the purposes that etherification reaction carries out dealkalize before.
Further set forth content of the present invention below in conjunction with drawings and Examples.
Description of drawings
Fig. 1 is C of the present invention
3～C
5Alkane carries out the process flow diagram of rotational flow alkali removing.
Fig. 2 is the C of prior art
3～C
5The process flow diagram of the dealkalization method of alkane (before transforming).
Wherein:
1---under meter;
2---liquid-liquid mixer;
3---slurry tank;
4---liquid liquid separator;
5---methanol tank;
6---feedstock pump (C
3～C
5Alkane);
7---methanol pump.
Embodiment
The inventor adopts the reaction conditions of particular combinations through extensive and deep research, thereby has solved in the reaction emulsification easily and be easy to generate a large amount of foamy problems.In a preferred embodiment, the contriver is surprised to find, and the use de-oxygenised water can reduce the chocking-up degree in the separating device greatly, has finished the present invention on this basis.
Term among the present invention " MTBE " ether-based device is meant that methyl tertiary butyl ether makeup puts.
Design of the present invention is such:
By being that the dealkalize water-dispersion of 0.1～5.0 parts by volume is mixed into the liquid C of 95～99.9 parts by volume with volume ratio
3～C
5Alkane (is C
3～C
5) in, this C
3～C
5The alkali that alkane is carried secretly passes to dealkalize water; Then, utilize liquid C
3～C
5Density difference between alkane, the two kinds of non soluble liquids of water relies on fluid high speed rotating in cyclone separator to produce centrifuge field with C
3～C
5Alkane and water sepn, water is taken alkali out of, thereby realizes the purpose of butane dealkalize.Obtained good alkaline impurities separating effect, so be particularly suitable as the preceding tripping device of ether-based device to prevent the poisoning of catalyst in the ether-based device.
In order to realize above-mentioned separation, make up the system of a transmittance process and cyclonic separation process combination.Transmittance process is by disperse lower salt content water in raw material, and alkaline matters such as water dissolution amine, alkali, alkalimetal ion, acetonitrile, propionitrile and nitride have realized that alkaline matter is from transfer and the enrichment process of raw material to water droplet.The cyclonic separation process makes the fluid rotation through the cyclone separator of special construction under given conditions, and the centrifuge field that rotational flow produces will contain the water droplet of alkaline matter to be separated from raw material, has realized that alkaline matter breaks away from the process of raw material.
At first, in transmission-cyclonic separation combined system, water and raw material blended facility are set, finish that water injection, water mix with the raw material disperse, raw material neutral and alkali material is to the enrichment process of water migration, water neutral and alkali material.Treat raw material and water thorough mixing, after alkaline matter and water fully transmitted, water and raw mix entered in the liquid-liquid rotational flow separation device.
Secondly, in transmission-cyclonic separation combined system, the facility of a liquid-liquid rotational flow separation is set, finishes rapidly and efficiently separating of alkaline water and raw material.Alkaline water is to sewage treatment facility.Raw material after the dealkalize enters reaction unit.
In a word, by above-mentioned measure, solved the MTBE device, gasoline etherification device raw material alkali content exceeds standard, caused an acidic catalyst life-span short, the problem that the device cycle of operation is long.
In a preference, enter methyltertiarvbutyl ether reactor (as the MTBE methyltertiarvbutyl ether reactor) at raw material a device integration system of being made up of liquid-liquid mixer, make-up water pump or band setting-out origin system, butane topping-up pump, slurry tank, Liquid-Liquid Separation Hydrocyclone is set before.
Below describe all respects of the present invention in detail.
C
3～C
5Alkane
Term " C among the present invention
3～C
5Alkane " be meant C
3, C
4, C
5Alkane or its combination.Be meant C especially
5The content of alkane is no more than the C of 10wt%
3, C
4, C
5The mixture of alkane is in the gross weight of alkane.C
3～C
5The example of alkane is including, but not limited to liquefied petroleum gas (LPG).
C described in the present invention
3～C
5Alkane can also include other organic impurities, as C
8Impurity etc., the content of these organic impurities is no more than C
3～C
5The 5wt% of alkane is with C
3～C
5The weight meter of alkane.
Term " C among the present invention
3Alkane " (being carbon three alkane) be meant that straight or branched is saturated or undersaturated, contain the one matter or the mixture of the alkane of 3 carbon atoms.For example, propylene, propane or its combination.
Term " C among the present invention
4Alkane " (being butane) be meant that straight or branched is saturated or undersaturated, contain the one matter or the mixture of the alkane of 4 carbon atoms.For example, the various isomer of the various isomer of butylene, butane or its combination.
Term " C among the present invention
5Alkane " (being C 5 alkane) be meant that straight or branched is saturated or undersaturated, contain the one matter or the mixture of the alkane of 5 carbon atoms.The for example various isomer and the combination thereof of the various isomer of propylene, butane.
Water-soluble alkaline impurity
Water-soluble alkaline impurity of the present invention comprises amine, alkali, alkalimetal ion, acetonitrile, propionitrile and nitride.Especially, described nitride is that hydrazine (hydrazine), morpholine and other are used for the solvent based of corrosion control, and these solvents are for making the basic nitrogen compound component of poisoning of catalyst.
The source of these water-soluble alkaline impurity is: petroleum chemical industry, carbon three, butane, C 5 alkane through the gas fraction device obtains then carry out subsequent reactions such as etherificate then.Above-mentioned carbon three alkane, butane, C 5 alkane are through taking off H
2S and mercaptan, remaining alkali lye material in the system is as amine, alkali, alkalimetal ion, acetonitrile, propionitrile and nitride.
The composition of described water-soluble alkaline impurity and content can be according to the component concentration fluctuations to some extent up and down of raw material.
Described amine, such as, but be not limited to: methylamine, ethamine, propylamine, hydramine or its combination.
Described alkali, such as, but be not limited to, NaOH, KOH etc.
Described alkalimetal ion, such as, but be not limited to: Li, Na, K ion.
Described nitride is that hydrazine (hydrazine), morpholine and other are used for the solvent based of corrosion control such as, but be not limited to: described nitride.
Particularly when follow-up etherification reaction adopts acidic cation-exchange resin to make catalyzer, be subject to the influence of materials such as charging neutral and alkali nitride, metallic cation and poisoning of catalyst.Studies show that there are following six kinds of mechanism in catalyst deactivation: physics inactivation, chemical inactivation, thermodynamics degraded, organic polymer fouling, positively charged ion inactivation, basic nitrogen compound hydrolytic inactivation.Wherein, the basic nitrogen compound hydrolytic inactivation be after nitrile in the charging (being mainly acetonitrile, the propionitrile) hydrolysis with catalyzer in the Zeo-karb catalyst deactivation that reacts and cause.The neutralization reaction of nitrile can be divided into for two steps: the first step, and the nitrile in the raw material is adsorbed in the resin, and adsorptive capacity depends on the partition ratio (partition coefficient) of nitrile between raw material and resin.Experiment shows, is present in methyl alcohol and nonactive C
4Nitrile in the hydrocarbon, under state of saturation, its amount of being adsorbed can reach 6kg/100kg resin (butt).In second step, nitrile that is adsorbed and water reaction at first generate aminocompound, generate organic acid and ammonia with the water reaction again, and the sulfonic group generation neutralization reaction in ammonium ion and the resin causes poisoning of catalyst.Water in the hydrolysis reaction has three places sources: the water that methyl alcohol or LCN carry, washing water and the methanol polymerized water that generates during for dme (DME).
The poisoning of catalyst that is caused by the acetonitrile hydrolysis is different from the first five kind situation, the poisoning that the first five kind situation causes all is a stepping type, promptly that part of poisoning of catalyst that at first contacts with reactant just can cause that part of poisoning of catalyst adjacent with poisoned catalyst then.The latter then is that basic nitrogen compound at first is adsorbed on whole beds, and then the reaction that is hydrolyzed, and causes the active decline of whole beds, therefore should the poisoning process have more hazardness.Nitrile compound content is as shown in table 1 to the influence in catalyst for etherification life-span.
Table 1 nitrile compound content is to the influence in catalyst for etherification life-span
| Nitrile compound content/μ g.g-1 | ＜1 | 3～15 | ＞30 |
| Catalyst life/a | 2 | 0.5～0.7 | ＜0.3 |
Dealkalize water
Dealkalize water of the present invention comprises de-mineralized water, de-oxygenised water and condensed water, is used for C
3～C
5Catalyzer poison in the alkane charging washes away.
Dealkalize water of the present invention meets the following conditions:
pH 5.5～9.5
Hardness, ppm CaCO
30.0～0.5
The total solids particle, ppm 0.5 ± 0.1
Silicon (SiO
2), ppm is no more than 0.2
Copper (Cu), ppm 0.01 ± 0.005
Iron (Fe), ppm 0.03 ± 0.02
Electric conductivity, ms/cm is no more than 0.5
Oxygen, ppm 0.005 ± 0.001
Sodium+potassium, ppm is no more than 0.2
Basic nitrogen compound, ppm is no more than 1.0
The definition of de-mineralized water of the present invention is: SiO
2Content is less than 0.1ppm, and Na+ content is less than 0.1ppm, and PH is 8.0-9.0, and specific conductivity is less than 10 μ s/cm.In a preference, the component of de-mineralized water satisfies following character:
pH 7.5～9.0
Hardness, ppm CaCO
30.0
The total solids particle, ppm 0.5
Silicon (SiO
2), ppm 0.02
Copper (Cu), ppm 0.01
Iron (Fe), ppm 0.02
Electric conductivity, ms/cm 0.5
Oxygen, ppm 0.005
Sodium+potassium, ppm 0.01
Basic nitrogen compound, ppm 1.0 (maximum)
In a preferred embodiment of the invention, adopt de-oxygenised water, wherein the component of de-oxygenised water and de-mineralized water are basic identical, and difference is that oxygen content is not more than 0.005ppm, particularly below 0.003ppm.The contriver finds, adopts de-oxygenised water can reduce the chocking-up degree of equipment greatly.The contriver thinks that reason is: the alkane after the desulfurization is entrained with hydramine (containing hydrogen sulfide).The separate object boiling point is lower in the present invention, during as carbon three, butane, hydramine is easy to form foam amine, and its surface-area increases, therefore be easy to and the oxygen effect generates organic acid and other unrenewable materials, and with reaction system in the alkaline matter generation salt that reacts.Adopt de-oxygenised water can prevent that it from carrying out oxidation and preventing to bring into promotion corrosive oxide compound and other impurity again simultaneously.Thereby solved easy blocking problem in the equipment.
In another preferred embodiment of the present invention, adopt condensed water.Condensed water is better than softened water quality, can be directly as technology water filling usefulness, and the value that reclaims 1 ton of water is about 10-15 unit.Reduced the water consumption, reduced the soda acid expense again, killed two birds with one stone.The water quality of condensed water is good, near de-salted water, and does not almost dissolve gases such as oxygen and carbon dioxide; The condensate depression of condensed water is smaller, near saturated.
Usually, the condense SiO of water pot
2Content is 0.06～0.08ppm, Na
+Content is 0.04～0.07ppm, and PH is 7.8-9.0, and specific conductivity is 2.4-6.0 μ s/cm.The example of condensed water is as shown in table 2 below:
The content of table 2 condensed water
| Time | Iron level ppm | Na + ppm | SiO 2 ppm | Specific conductivity μ S/cm | PH |
| | 0.046 | 0.049 | 0.067 | 6.9 | 9.1 |
| | 0.033 | 0.069 | 0.121 | 7.4 | 8.9 |
| | 0.045 | 0.147 | 0.056 | 8.1 | 9.0 |
| Condensed water #4 | 0.037 | 0.51 | 0.159 | 7.3 | 9.2 |
| | 0.038 | 0.169 | 0.089 | 6 | 9.3 |
Liquid-liquid mixer
Liquid-liquid mixer of the present invention is meant said raw material and water blended, can be a kind of in conventional static mixer, micro-mixer, stirring mixer, squirt pump, the Venturi-type mixing tank etc., preferred static mixer; Internals at static mixer are taked anti-corrosive treatment, as surperficial corrosion-resistance treatment or selection corrosion resistant material, to improve the work-ing life of mixing tank, ensure mixed effect.
Cyclone separator
Liquid-liquid rotational flow separation device of the present invention can be a kind of in improved whirlwind-type water-and-oil separator, coarse water-and-oil separator, the eddy flow-jet-coarse water-and-oil separator; The whirlwind-type water-and-oil separator is the core internals-available bipyramid of eddy flow core pipe of cyclone separator, two feeding inlet structure, single cone, two feeding inlet structure, single cone, single feeding inlet structure, ultrashort tail pipe or anury tubular construction, and two opening for feed, three cone structures.
The structure of the eddy flow core pipe in the described cyclone separator comprises: the two feeding inlet structures of bipyramid, the two feeding inlet structures of single cone, the single feeding inlet structure of single cone, ultrashort tail pipe or anury tubular construction or the two feeding inlet structures of three cones.
The mounting means of cyclone separator of the present invention can be vertical or horizontal.
The pressure of cyclone separator of the present invention falls between 0.06～0.1MPa, also can reach isolating effect.
Below in conjunction with specific embodiment, further illustrate the present invention.Should be understood that these embodiment only to be used to the present invention is described and be not used in and limit the scope of the invention.The experimental technique of unreceipted actual conditions in the following example, usually according to normal condition, or the condition of advising according to manufacturer.Ratio and per-cent are based on weight, unless stated otherwise.The symbol of the content of ppm (also being expressed as PPM) expression micro substance in mixture refers to umber or PPM (branch weight ratio PPMw and volume ratio PPMv) in each 1,000,000 parts.The said ppm of the present invention is a weight ratio.1ppm promptly contains 1 kilogram of solute in the solution of 100 kilograms.1ppm is equivalent to 1ug/ml, also is equivalent to 1mg/l.
In the butane etherificate MTBE of 100,000 tons of yearly capacities device, the method for conceiving according to the present invention is provided with a method of overlapping butane transmission-rotational flow alkali removing, and its concrete operation and effect are described below:
Referring to Fig. 1, before butane enters the reaction process of MTBE device, start water pump 1, the condensed water atomizing with 0.5% is also injected static mixer 2, through static mixer 2 the water disperse is mixed in the butane raw material, it is the drop of 20 μ m～50 μ m that described condensed water forms median size.Afterwards through the suitably long time, water-soluble alkaline matter in the butane as amine, alkali, alkalimetal ion, acetonitrile, propionitrile and nitride etc., is delivered in the water droplet of disperse.Mix with described alkane again.Raw material directly enters gravity settler 3 from the outlet of static mixer 2, gravity settler 3 will not have the water of disperse and oarse-grained water droplet to separate, these water carry part alkali and are transported to Sewage treatment systems from pressing, and the small-particle water droplet directly enters with the butane raw material or enters rotational flow alkali removing device 4 through butane feedstock pump 6.Rotational flow alkali removing device 4 is separated little water droplet from the butane raw material, little water droplet carries most of alkali from compressing into into Sewage treatment systems, and the butane of deviating from alkali lye is respectively as the raw material of producing MTBE.
Measurement result shows: the present invention has solved butane dealkalize problem in the butane etherification procedure effectively, an acidic catalyst of etherification procedure is delayed or avoids poisoning, and prolongs the work-ing life of catalyzer, ensures the long-term operation of MTBE device.
Contrast effect is summarized as follows before and after transforming:
1. water consumes: before the transformation: 0%; (referring to Fig. 2)
The catalyst life cycle: before the transformation: 50 days;
Only through gravity settler, the situation of 3～4 grades of copper corrosions often occurs, qualification rate is 10%～50%.Cause a large amount of races of amine liquid to decrease simultaneously (run and decrease amine liquid total amount more than 200t/a).For addressing this problem, methods such as washing, sedimentation, coalescence filtration have been adopted, all because a variety of causes does not reach the ideal effect.
2. transform the back: increase water 0.1～0.5% (wt)
The catalyst life cycle: 90 days.
In a word, adopt method of the present invention, solved the problem that raw material is carried alkali lye secretly reliably, delayed catalyst life, prolonged the system stable operation cycle.
Therefore: adopt method of the present invention, solved at C fairly perfectly
3～C
5In the alkane etherification procedure, because raw material is carried alkaline matter secretly, cause an acidic catalyst to be poisoned, device is short running period, the running cost height, the problem that whole plant investment is high realizes that promptly the degree of depth of raw material neutral and alkali material is deviate from, an acidic catalyst life-span prolongs, device prolongs running period, thereby has advanced the process of industrialization of petrochemical complex cleaner production effectively.
Technology suitability of the present invention is good, and is stable, efficient, the ripe easily row of operation control, and less investment, facility compact, working cost is low, can the operation of long period steady and continuous.The present invention is specially adapted to the lower system of boiling point such as carbon three, butane etherificate, C 5 alkane etherificate.The very low liquid/liquid of immiscible or solubleness that also can be applied to oil refining such as pimelinketone, LPG Desulfurization, oily desalination, gasoline etherification, chemical plant installations separates.
1. treatment condition:
20～100 ℃ of temperature, treatment capacity 0.4-0.8m
3/ h, liquefied gas characteristic: density 600kg/m
3,
Viscosity 0.14mPa.s.Amine liquid density 1040kg/m
3, concentration 1300-1800mg/l
2. analytical procedure is with the amine liquid hold-up in the legal property of the copper corrosion analytic liquid gasification sample, with the amine liquid hold-up in the slow method of evaporation quantitative analysis of the Li Senke bottle liquefied gas sample
3. effect
(1) disengaging time is short, and 1～2s can isolate.Major part about 20 μ m is separated from tail pipe.
(2) take off amine efficient more than 94%, reach maximum 99% about 600l/h, amine liquid drops to below the 99mg/l from 1800mg/l.
(3) isolated amine liquid is black, and this is owing to wherein contain due to the tiny solid particulate matter, but swirler is stable, does not stop up.
(4) pressure drop has only 0.1Mpa on the swirler, and energy consumption is very low.
Single optimum flow 0.9-1.6m
3/ h selects the use in parallel of 65 cyclone pipes for use
1. treatment condition:
20～100 ℃ of temperature, treatment capacity 58.5-104m
3/ h, liquefied gas characteristic: density 522kg/m
3,
Viscosity 0.107mPa.s.Amine liquid density 1018kg/m
3, viscosity 0.107mPa.s,
Concentration 106-780mg/l
2. analytical procedure is with the amine liquid hold-up in the legal property of the copper corrosion analytic liquid gasification sample, with the amine liquid hold-up in the slow method of evaporation quantitative analysis of the Li Senke bottle liquefied gas sample
3. effect
(1) contain amine liquid measure level between 106-780mg/l the time in the import liquefied petroleum gas (LPG), it is 22-99mg/l that the outlet liquefied petroleum gas (LPG) contains the amine liquid measure,
(2) amine liquid separation efficiency is 67% to 95%, and average separation efficiency is 87.6%,
(3) isolated amine liquid is water sample liquid, little green that is.To carrying out copper strip test through the liquefied petroleum gas (LPG) sampling that purifies, it is qualified to be.
(4) pressure drop is between 0.06～0.1Mpa.
(5) reach 80% amine liquid organic efficiency.
All quote in this application as a reference at all documents that the present invention mentions, just quoted as a reference separately as each piece document.Should be understood that in addition those skilled in the art can make various changes or modifications the present invention after having read above-mentioned teachings of the present invention, these equivalent form of values fall within the application's appended claims institute restricted portion equally.
Claims (10)
1, a kind of method of rotational flow alkali removing is characterized in that, may further comprise the steps:
(a) C that contains water-soluble alkaline impurity of 95～99.9 parts by volume
3～C
5The dealkalize water of alkane and 0.1～5.0 parts by volume is at 20～120 ℃, and 0.01MPa～0.50MPa mixes down, obtains the mixture that water content is 10000mg/L～50000mg/L,
Wherein said water-soluble alkaline impurity accounts for 1～30wt% of described alkane weight,
(b) the centrifugal rotation of mixture that obtains of step (a) separates, and obtains the alkane of dealkalize.
2, method according to claim 1 is characterized in that, described water-soluble alkaline impurity is amine, alkali, alkalimetal ion, acetonitrile, propionitrile, nitride and combination thereof.
3, method according to claim 1 is characterized in that, described dealkalize water is de-mineralized water, de-oxygenised water or condensed water.
4, method according to claim 1 is characterized in that, it is after the drop of 20 μ m～50 μ m that the described dealkalize water of step (a) forms median size earlier, mixes with described alkane again.
5, a kind of rotational flow alkali removing device of method employing according to claim 1 is characterized in that, comprises water injection equipment, liquid-liquid mixer and cyclone separator,
Described water injection equipment is located at the upstream of described liquid-liquid mixer, and described swirler separator is located at the downstream of described liquid-liquid mixer.
6, device according to claim 5 is characterized in that, the downstream of described cyclone separator also is provided with waste disposal plant.
7, device according to claim 5 is characterized in that, described cyclone separator pressure is reduced to 0.05MPa～0.25MPa.
8, device according to claim 5 is characterized in that, also is provided with settling vessel between liquid-liquid mixer and cyclone separator.
9, a kind of MTBE ether-based device, the wherein described rotational flow alkali removing device of the with good grounds claim 5 of the provided upstream of MTBE methyltertiarvbutyl ether reactor.
10, the described device of method according to claim 1 or claim 6 is at C
3～C
5Alkane carries out the purposes that etherification reaction carries out dealkalize before.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260525A (en) * | 2011-06-17 | 2011-11-30 | 华东理工大学 | Gasoline dealkalizing device and use method thereof |
| CN102433159A (en) * | 2011-09-22 | 2012-05-02 | 凯瑞化工股份有限公司 | Catalytic gasoline light fraction etherification process |
| CN101485947B (en) * | 2008-12-30 | 2012-06-27 | 华东理工大学 | Method and device for removing micro-phase alkaline matter in fluid |
| CN106947563A (en) * | 2017-05-09 | 2017-07-14 | 天津亿利科能源科技发展股份有限公司 | A kind of production method of low-corrosiveness liquefied petroleum gas |
| CN115487951A (en) * | 2022-11-01 | 2022-12-20 | 天津德通电气有限公司 | Medium removal sieve material flow break identification method and system |
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2006
- 2006-04-13 CN CNB2006100256757A patent/CN100535085C/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101485947B (en) * | 2008-12-30 | 2012-06-27 | 华东理工大学 | Method and device for removing micro-phase alkaline matter in fluid |
| CN102260525A (en) * | 2011-06-17 | 2011-11-30 | 华东理工大学 | Gasoline dealkalizing device and use method thereof |
| CN102433159A (en) * | 2011-09-22 | 2012-05-02 | 凯瑞化工股份有限公司 | Catalytic gasoline light fraction etherification process |
| CN102433159B (en) * | 2011-09-22 | 2014-04-02 | 凯瑞化工股份有限公司 | Catalytic gasoline light fraction etherification process |
| CN106947563A (en) * | 2017-05-09 | 2017-07-14 | 天津亿利科能源科技发展股份有限公司 | A kind of production method of low-corrosiveness liquefied petroleum gas |
| CN115487951A (en) * | 2022-11-01 | 2022-12-20 | 天津德通电气有限公司 | Medium removal sieve material flow break identification method and system |
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| CN100535085C (en) | 2009-09-02 |
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