CN212387999U - Light hydrocarbon sweetening alkali liquor regeneration system - Google Patents
Light hydrocarbon sweetening alkali liquor regeneration system Download PDFInfo
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- CN212387999U CN212387999U CN202021608427.7U CN202021608427U CN212387999U CN 212387999 U CN212387999 U CN 212387999U CN 202021608427 U CN202021608427 U CN 202021608427U CN 212387999 U CN212387999 U CN 212387999U
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Abstract
The utility model discloses a light hydrocarbon desulfurization alcohol alkali liquor regeneration system, which comprises a step I of carrying out microfiltration or ultrafiltration treatment (such as ceramic membrane filtration) on desulfurization alcohol alkali liquor to be treated; step two, carrying out (two-compartment) bipolar membrane electrodialysis treatment on the filtered alkali liquor to obtain recovered alkali liquor and feed liquid with the pH value less than or equal to 8; thirdly, acidifying the feed liquid with the pH value less than or equal to 8, wherein the pH value of the acidified feed liquid is less than or equal to 5; neutralizing the acidified feed liquid by using alkali to obtain basic neutral feed liquid containing strong alkali and strong acid salt; and step five, carrying out (three-compartment) bipolar membrane electrodialysis treatment on the neutral feed liquid to obtain strong acid liquid, strong alkali liquid and low-concentration salt-containing water.
Description
Technical Field
The utility model relates to a petrochemical technical field, concretely relates to light hydrocarbon sweetening alkali lye regeneration system.
Background
Hydrocarbons are a generic term for hydrocarbons, and generally, hydrocarbons having less than 7 carbon atoms in the hydrocarbon molecule are light hydrocarbons. The main component of common natural gas is methane (also known as C1 hydrocarbon, where "C" refers to carbon atoms and the number of carbon atoms in the "1" molecule). The main components of the refinery gas generated in the petroleum refining process are C1 and C2 hydrocarbons. The main components of the liquefied gas produced in the petroleum refining process are C3 and C4 hydrocarbons. Gasoline is mainly C5-C12 hydrocarbon. The C1-C4 hydrocarbon is gas at normal temperature and normal pressure and is generally called gaseous light hydrocarbon. The C5-C10 hydrocarbon is liquid at normal temperature and pressure, and is generally called liquid light hydrocarbon or the like.
Light hydrocarbons are produced in petroleum refining, coal chemical industry and other industries. The sulfides in the light hydrocarbon mainly comprise hydrogen sulfide, mercaptan, thioether, thiophene sulfides and the like. The sulfide is necessary to be removed because the sulfide can generate corrosion and pollution in the deep processing or using process of the light hydrocarbon.
The existing light hydrocarbon sweetening process mainly comprises fixed bed sweetening, solvent extraction sweetening and alkali liquor extraction oxidation regeneration sweetening, wherein the alkali liquor extraction oxidation regeneration process has strong raw material adaptability, low operation cost, good sweetening effect and the most extensive application.
In the alkali liquor extraction oxidation regeneration process, the soluble salts in the alkali liquor comprise mercaptan and CO brought by raw material light hydrocarbon2、H2Soluble salts generated by the reaction of acidic substances such as S and the like with alkali, and soluble salts generated by the reaction of acidic substances with alkali brought by oxidation wind, reverse extraction oil and the like of a regeneration unit. Wherein, the thiolate reacts with oxygen in the oxidizing air under the action of the catalyst to generate disulfide and alkali, the disulfide is separated out of the system, and the regenerated alkali can be recycled. But due to CO2、H2The salt generated by the reaction of acidic substances such as S and the like and alkali cannot be completely regenerated in the oxidation regeneration link, so that the content of miscellaneous salt in the solution of the system is increased, the normal operation of light hydrocarbon sweetening is finally influenced, the salt has to be treated in a new alkali replacement mode, the withdrawn high-salt-content sulfur-containing alkali liquor with insufficient sweetening activity is called as alkaline residue, the alkali concentration is even as high as about 10 percent, and the alkaline residue is treated as hazardous waste. The difficulty of caustic sludge treatment is high, most enterprises can only spend money by qualified units without capacity treatment, and the qualified units have high charge and limited treatment capacity, so that the treatment of liquefied gas sweetening caustic sludge is a difficult problem which troubles the enterprises.
Accordingly, there is a need for new techniques and methods to at least partially address the problems of the prior art.
SUMMERY OF THE UTILITY MODEL
The method can completely regenerate the alkali liquor in the prior art by the combined technologies of ceramic membranes (such as a filtering unit), bipolar membranes, monopolar membranes (such as an alkali concentrating unit and an acid concentrating unit), and the like, particularly carbonate which cannot be regenerated by a wet oxidation sweetening process and has large content can be dissociated to generate alkali and carbon dioxide. The method is green and environment-friendly, and provides a new idea for regenerating the liquefied gas sweetening alkali liquor.
According to an aspect of the utility model, a method for light hydrocarbon desulfurization alcohol alkali liquor regeneration is provided, including following step:
step one, performing microfiltration or ultrafiltration treatment (for example, filtration by using a ceramic membrane can be used but not limited to) on the desulfurized alcohol alkali liquor to be treated;
step two, carrying out (two-compartment) bipolar membrane electrodialysis treatment on the filtered alkali liquor to obtain recovered alkali liquor and feed liquid with the pH value less than or equal to 8;
thirdly, acidifying (sulfuric acid) the feed liquid with the pH value less than or equal to 8, wherein the pH value of the acidified feed liquid is less than or equal to 5;
neutralizing the acidified feed liquid by using alkali to obtain basic neutral feed liquid containing strong alkali and strong acid salt; and
and fifthly, performing (three-compartment) bipolar membrane electrodialysis treatment on the neutral feed liquid to obtain strong acid liquid, strong alkali liquid and light saline.
Preferably, the method further comprises the step of performing acid recovery treatment on the feed liquid with the pH value less than or equal to 8 by using a (two-compartment) bipolar membrane before the step three to obtain weak acid liquid and residual liquid, wherein the residual liquid is subjected to acidification treatment in the step three; for example, the weak acid, such as carbonic acid, may be removed as carbon dioxide gas and the liquid organic weak acid may be treated in an extraction mode.
Preferably, the method further comprises filtering the neutral feed solution before step five.
Preferably. Wherein in the third step, gaseous products are generated, and the gaseous products comprise carbon dioxide and small molecule mercaptan.
Preferably, the method further comprises the step of performing alkali concentration on the recovered lye of the step two and/or the strong lye of the step five.
Preferably, the method further comprises a step of acid concentrating the strong acid solution of the step five or a step of acid concentrating the weak acid.
Preferably, the method further comprises the step three of acidizing by using the strong acid solution in the step five.
Preferably, the method further comprises the neutralization of the fourth step by using the strong alkali liquor in the fifth step.
Preferably, the method further comprises adding the salt-containing water obtained in step five as a make-up water to step two and step five.
According to the utility model discloses an on the other hand provides a light hydrocarbon sweetening alkali lye regeneration system, include:
the first filtering unit is used for carrying out microfiltration or ultrafiltration treatment (ceramic membrane filtration) on the desulfurized alcohol alkali liquor to be treated;
the alkali recovery unit is used for carrying out (two-compartment) bipolar membrane electrodialysis treatment on the filtered alkali liquor to obtain recovered alkali liquor and feed liquid with the pH value less than or equal to 8;
the acidification unit is used for carrying out acidification (sulfuric acid) treatment on the feed liquid with the pH value less than or equal to 8, and the pH value of the acidified feed liquid is less than or equal to 5;
a neutralization unit, which is used for neutralizing the acidified feed liquid by alkali to obtain basic neutral feed liquid containing strong alkali strong acid salt; and
and the salt decomposition unit is used for carrying out (three-compartment) bipolar membrane electrodialysis treatment on the neutral feed liquid to obtain strong acid liquid, strong alkali liquid and light saline.
Preferably, the system further comprises an acid recovery unit, before the acidification unit is arranged, the feed liquid with the pH value less than or equal to 8 is subjected to acid recovery treatment by using a (two-compartment) bipolar membrane to obtain weak acid liquid and residual liquid, and the residual liquid enters the acidification unit for treatment.
Preferably, the system further comprises a second filtering unit disposed before the salinity decomposition unit for filtering the neutral feed liquid.
Preferably, the system further comprises an acid concentration unit for acid concentration of the acid produced by other units in the system.
Preferably, the system further comprises a base concentration unit for performing base concentration on the base produced by other units in the system.
The utility model solves the problem that the alkali liquor can not be completely regenerated in the prior art of removing mercaptan from light hydrocarbon by alkali extraction. The method solves the problem that the concentration of the effective alkali in the process of light hydrocarbon alkali extraction and sweetening is continuously reduced, and also solves the problem that the alkaline residue of enterprises is difficult to treat. Not only saves the cost of alkali liquor consumption, but also saves the cost of treating the alkaline residue.
Drawings
Some specific embodiments of the present invention will be described in detail hereinafter, by way of illustration and not by way of limitation, with reference to the accompanying drawings. The same reference numbers in the drawings identify the same or similar elements or components. In the drawings:
FIG. 1 is a schematic flow diagram of a process for regenerating light hydrocarbon sweetening alkali liquor according to an embodiment of the present invention.
Detailed Description
The technical solution of the present invention will be further clearly and completely described below with reference to the accompanying drawings and examples, and it should be understood that the examples are intended to illustrate the present invention and help those skilled in the art to better understand the present invention, but not to limit the present invention.
As shown in the figure, the regeneration method of light hydrocarbon sweetening alkali liquor of the embodiment of the present invention may include the steps of first filtering, alkali recovery, acid recovery, acidification, neutralization, second filtering, salt decomposition, acid concentration, alkali concentration, etc.
More specifically, the desulfurized alcohol lye to be treated (hereinafter referred to as the raw material) is introduced into the first filtering unit for filtering, and impurities such as suspended matters in the raw material are removed. The first filtration unit may be a microfiltration or ultrafiltration device, such as a ceramic membrane or the like. The raw material mainly contains a strong alkali salt, a weak alkali salt, and other salts, such as sodium hydroxide, sodium carbonate, sodium sulfate, sodium sulfide, and the like.
After filtration, the filtrate enters an alkali recovery unit for alkali recovery. The alkali recovery unit may be a two-compartment bipolar membrane electrodialysis treatment unit in which the alkali liquor, e.g. sodium hydroxide solution, is mainly recovered. The recovered alkali liquor enters an alkali concentration unit for concentration and then is recovered; the other feed liquid of the alkali recovery unit has a pH value less than or equal to 8 and can contain sodium carbonate, sodium sulfate and the like, and the feed liquid is introduced into the acid recovery unit.
The acid recovery unit may be a two-compartment bipolar membrane electrodialysis treatment unit. In the unit, weak acid (such as mercaptan, formic acid, etc.) in the feed liquid with the pH value less than or equal to 8 is separated through the action of an electrically driven membrane and can enter an acid concentration unit; the rest material liquid enters an acidification unit for treatment. It should be understood that the acid recovery unit may be selectively positioned as desired, for example, the acid recovery unit may be positioned such that the feed solution having a pH of 8 is introduced directly into the acidification unit.
After the liquid material enters the acidification unit, strong acid such as sulfuric acid or other suitable strong acids is used for processing, so that weak acid in the liquid material is removed, generated carbon dioxide, micromolecule mercaptan and the like are discharged in a gaseous state, the liquid material is processed along with waste gas, and the pH value of the acidified liquid material is less than or equal to 4. The acidification treatment can be carried out by using strong acid (such as sulfuric acid) generated by the salt decomposition unit, and the internal circulation can save raw materials and cost and reduce the discharge of waste. Specifically, during the acidification process, carbonate reacts with strong acid to generate, for example, strong acid salt and carbon dioxide; in addition, the sulfides contained in the feedstock may react to form small molecule mercaptans, such as methyl mercaptan, ethyl mercaptan, and the like.
The feed liquid after acidification treatment mainly comprises sulfate, sulfuric acid and the like, enters a neutralization unit and is neutralized by alkali to obtain basically neutral feed liquid containing strong alkali strong acid salt such as sulfate. For example, the alkali (such as sodium hydroxide) generated by the subsequent salt decomposition unit can be utilized for neutralization, so that the internal circulation of materials can be realized, the raw materials and the cost can be saved, and the discharge of waste can be reduced.
And the neutralized feed liquid enters a second filtering unit and is filtered by an ultrafiltration membrane to remove impurities such as suspended matters and the like. The second filter unit may be selectively provided as needed. After filtration, the feed liquid enters a salt decomposition unit.
The salt splitting unit may be a three-compartment bipolar membrane electrodialysis treatment unit. The strong acid and strong base salts can be converted to strong acids and bases by treatment with a salt splitting unit, for example to form sulfuric acid and sodium hydroxide. The strong base can be introduced into a neutralization unit for recycling, and can also be introduced into a base concentration unit for further treatment. The strong acid can be introduced into an acidification unit for recycling, and can also be introduced into an acid concentration unit for further treatment. The light salt water produced by the salt chamber can be used as the water supplement for the acid chamber and the alkali chamber of the salt decomposition unit, the alkali chamber of the alkali recovery unit and the concentrated alkali chamber of the concentration unit, and can also be used as the salt-containing sewage discharged from a sewage treatment plant; because the salt in the salt chamber solution enters into the acid and the alkali respectively in the form of anion and cation, the salt content of the salt chamber solution is low, for example, the concentration can be lower than 1%, thereby being used for other purposes.
The alkali liquor from the alkali recovery and salt decomposition unit can be further concentrated in an alkali concentration unit, for example, by electrodialysis, and then 10% -30% concentrated alkali can be obtained. The concentrated alkali liquor can be sent to a mercaptan removal device for recycling, and the concentration of the concentrated alkali can be determined according to downstream requirements. The make-up liquid of the strong alkali chamber can be light saline water of the salt decomposition unit, and can also be desalted water by the system.
The acid solution from the salt decomposition unit may enter an acid concentration unit for further concentration, for example, electrodialysis concentration may be performed, and then 10% to 30% concentrated acid may be obtained, and the concentrated acid solution may be sent out of the apparatus as a product. The concentration of the concentrated acid can be determined as desired. The make-up fluid of the concentrated acid chamber can be the light saline water of the salt decomposition unit, and can also be the desalted water of the system.
Examples
The embodiments are intended to be illustrative of the invention, rather than limiting; more specifically, utilize the utility model discloses a system handles sweetening alcohol alkali lye (raw materials), and this system includes: a first filtration unit (ceramic membrane ultrafiltration), an alkali recovery unit (two-compartment bipolar membrane electrodialysis), an acid recovery unit (two-compartment bipolar membrane electrodialysis), an acidification unit, a neutralization unit (using the strong base produced by the salt decomposition unit), a second filtration unit (ceramic membrane ultrafiltration), a salt decomposition unit (three-compartment bipolar membrane electrodialysis), an acid concentration unit (electrodialysis) and an alkali concentration unit (electrodialysis).
The raw material components are as follows: mainly comprises 3-10% of sodium hydroxide, 3-18% of sodium carbonate, 1-5% of sodium sulfate and less than 0.01% of sodium sulfide; 0.1-0.5% of sodium thiosulfate;
the operating parameters of each unit and the main components and concentrations after treatment are as follows in tables 1 and 2:
TABLE 1 (calculated from the initial amount of the raw material 100 Kg)
TABLE 2
The method takes 'mercaptan removal alkali liquor to be treated' as a raw material, takes 'purified mercaptan removal alkali liquor' as a product, takes 'product acid' as a byproduct, and takes reaction gases such as carbon dioxide generated by decomposing carbonate and the like as exhaust 'waste gas'. The production of the by-products depends on the needs of the enterprise, and the composition and amount of the by-products and off-gases depend on the raw carbonate and other impurity levels. When the waste gas mainly consists of carbon dioxide, the waste gas can be directly discharged into a low-pressure gas system or directly discharged after being treated by sodium carbonate and other solutions. When the waste gas contains more mercaptan sulfide, it is absorbed by absorption oil (gasoline or diesel oil) and then hydrogenated with the absorption oil. The utility model solves the problem that the alkali liquor can not be completely regenerated in the prior art of removing mercaptan from light hydrocarbon by alkali extraction. The method solves the problem that the concentration of the effective alkali in the process of light hydrocarbon alkali extraction and sweetening is continuously reduced, and also solves the problem that the alkaline residue of enterprises is difficult to treat. Not only saves the cost of alkali liquor consumption, but also saves the cost of treating the alkaline residue.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. The utility model provides a light hydrocarbon takes off mercaptan alkali lye regeneration system which characterized in that includes:
the first filtering unit is used for carrying out microfiltration or ultrafiltration treatment on the desulfurized alcohol alkali liquor to be treated;
the alkali recovery unit is used for carrying out two-compartment bipolar membrane electrodialysis treatment on the filtered alkali liquor to obtain recovered alkali liquor and feed liquid with the pH value less than or equal to 8;
the acidification unit is used for carrying out acidification treatment on the feed liquid with the pH value less than or equal to 8, and the pH value of the acidified feed liquid is less than or equal to 5;
a neutralization unit, which is used for neutralizing the acidified feed liquid by alkali to obtain basic neutral feed liquid containing strong alkali strong acid salt; and
and the salt decomposition unit is used for carrying out three-compartment bipolar membrane electrodialysis treatment on the neutral feed liquid to obtain strong acid liquid, strong alkali liquid and light saline.
2. The system of claim 1, further comprising an acid recovery unit, wherein before the acidification unit is arranged, the feed liquid with pH value less than or equal to 8 is subjected to acid recovery treatment by using a two-compartment bipolar membrane to obtain weak acid liquid and residual liquid, and the residual liquid enters the acidification unit for treatment.
3. The system of claim 1, further comprising a second filtration unit disposed before the salinity unit to filter the neutral feed liquid.
4. The system of claim 1, further comprising an acid concentration unit for acid concentration of acid produced by other units in the system.
5. The system of claim 1, further comprising a base concentration unit for base concentration of the base produced by other units in the system.
6. The system of claim 1, wherein the salt splitting unit is coupled to the acidification unit to deliver the strong acid solution of the salt splitting unit to the acidification unit.
7. The system of claim 1, wherein the salt splitting unit is connected to the neutralization unit to deliver strong lye of the salt splitting unit to the neutralization unit.
8. The system of claim 1, wherein the salt splitting unit is coupled to the soda recovery unit to deliver the saltwater of the salt splitting unit to the soda recovery unit.
9. The system of claim 4, wherein the salt splitting unit is coupled to the acid concentration unit to deliver the saltwater of the salt splitting unit to the acid concentration unit.
10. The system of claim 5, wherein the salt splitting unit is coupled to the base concentration unit to deliver the saltwater of the salt splitting unit to the base concentration unit.
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| CN111778061A (en) * | 2020-08-05 | 2020-10-16 | 伯尔菲特沧州科技中心 | Method and system for regenerating light hydrocarbon desulfurization alcohol alkali liquor |
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| CN111778061A (en) * | 2020-08-05 | 2020-10-16 | 伯尔菲特沧州科技中心 | Method and system for regenerating light hydrocarbon desulfurization alcohol alkali liquor |
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