CN202446974U - Combination system for removing mercaptan from liquefied gas - Google Patents
Combination system for removing mercaptan from liquefied gas Download PDFInfo
- Publication number
- CN202446974U CN202446974U CN2012200126538U CN201220012653U CN202446974U CN 202446974 U CN202446974 U CN 202446974U CN 2012200126538 U CN2012200126538 U CN 2012200126538U CN 201220012653 U CN201220012653 U CN 201220012653U CN 202446974 U CN202446974 U CN 202446974U
- Authority
- CN
- China
- Prior art keywords
- washing
- gas
- connects
- pipe
- oxidation
- Prior art date
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- 239000007789 gases Substances 0.000 title claims abstract description 185
- 239000003513 alkali Substances 0.000 claims abstract description 184
- 239000007788 liquids Substances 0.000 claims abstract description 125
- 230000003647 oxidation Effects 0.000 claims abstract description 72
- 238000007254 oxidation reactions Methods 0.000 claims abstract description 72
- 150000001412 amines Chemical class 0.000 claims abstract description 39
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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- 229910001890 sulfur dioxide Inorganic materials 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-N Carbonic acid Chemical group 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Abstract
Description
Technical field
The utility model relates to a kind of combined system of liquid gas sweetening.
Background technology
Remove in the liquefied gas (LPG) and contain H 2S, CS 2Outside acidic components, also contain some such as organic sulfurs such as mercaptan, thioether, COS, particularly wherein mercaptan because the severe toxicity and have volatility, corrosivity and nauseating bad odor, thereby environment is caused great pollution.Along with the poor qualityization of crude oil, complicated, and improve constantly what the liquefied gas product quality required, the liquefied gas of all kinds of device productions of oil plant is faced with all that total sulfur constantly raises, the more harsh trend of product liquefied gas total sulfur index.It is qualified to adopt traditional liquid gas sweetening technology (caustic prescrub depriving hydrogen sulphide+packed extraction column caustic wash desulfuration alcohol+water washing tank dealkalize+sand tower dehydration+filler oxidizing tower+disulphide knockout drum+alkali solution cooler) to be difficult to assurance total sulfur and mercaptans content.The subject matter that former technology exists is:
(1) liquefied gas sulfur-bearing total amount is higher and unstable behind the removal of mercaptans, and desulfurization degree is 40% ~ 80%.The product total sulfur content is lower when changing new alkali lye, but after 3～5 days, if do not change caustic prescrub alkali lye, then the product total sulfur content progressively rises; After alkali lye recycles 1 ~ 3 month, even the product total sulfur content under the prerequisite of frequent change caustic prescrub alkali lye, also is difficult to stably reaching standard.
(2) countermeasure of LPG sheet copper corrosion qualification rate low (30% ~ 40%).
(3) during the alkali liquid regeneration recycle, wherein accessory substance disulphide is difficult to from liquid phase separation, causes the alkaline residue discharge capacity big.
(4) disulphide gets into the incinerator burning with tail gas, often causes stench, and environmental protection drops into bigger.
(5) amine liquid is carried secretly often relatively more seriously during depriving hydrogen sulphide, and polluting alkali lye also increases alkali lye consumption.
(6) the alkaline sewage discharge capacity is big, needs long-time sedimentation separation water, and will pass through sand filtration and could guarantee that no free water carries secretly.
Therefore traditional liquid gas sweetening technology not only consumes and wastes a large amount of alkali lye; And produce a large amount of waste soda residues; Along with the raising of oil-refining chemical production environmental protection appraisal standards, traditional caustic wash desulfuration alcohol technology is more and more restricted, and new mercaptan removal technique reform is extremely urgent.
The utility model content
The purpose of the utility model provides a kind of combined system of liquid gas sweetening; Be used for sloughing the impurity such as amine liquid, hydrogen sulfide, mercaptan, alkaline matter of liquefied gas, make the residual sulphur rate in the liquefied gas reach GB or industry standard, and the alkali lye behind the removal of mercaptans can recycling utilization; The isolated disulphide of oxidation is delivered to the oil hydrogenation device can be converted into hydrogen sulfide; The final sulphur that generates has increased economic benefit, has overcome the above-mentioned deficiency of existing product in the market.
The purpose of the utility model is to realize through following technical scheme:
A kind of combined system of liquid gas sweetening; Comprise amine liquid coalescing separator, one-level liquid film sweetening reaction device, secondary liquid film sweetening reaction device, liquid film washing contactor, oxidation knockout tower, alkali lye stripping tower, disulphide jar, tail gas washing dealkalize jar, tail gas washing digester, membrane separator and tail gas oxidation sweetening jar; Be provided with the liquefied gas fine filter between said amine liquid coalescing separator and the one-level liquid film sweetening reaction device; One-level liquid film sweetening reaction device bottom connects first grade desulfurizing alcohol knockout drum through flange; Be provided with the alkali lye heat exchanger between first grade desulfurizing alcohol knockout drum and the oxidation knockout tower; Be provided with the catalyst injector between oxidation knockout tower and the alkali lye stripping tower; Said first grade desulfurizing alcohol knockout drum connects secondary liquid film sweetening reaction device through liquefaction tracheae behind the first grade desulfurizing alcohol; Secondary liquid film sweetening reaction device top is connected with into secondary removal of mercaptans alkali liquor pipe; Secondary liquid film sweetening reaction device bottom connects secondary removal of mercaptans knockout drum through flange, and secondary removal of mercaptans knockout drum connects liquid film washing contactor through liquefaction tracheae behind the secondary removal of mercaptans, and liquid film washing contactor bottom connects the washing knockout drum through flange; Said oxidation knockout tower top is put forward offgas duct through oxic gas and is connected the gas distributor one in the tail gas washing dealkalize jar; Tail gas washing dealkalize tank top through the washing dealkalize after offgas duct connect the gas distributor two in the tail gas washing digester, tail gas washing desulfurization tank top through the washing desulfurization after offgas duct junctional membrane separator, be provided with polymeric membrane in the membrane separator; The membrane separator top is separated the back offgas duct through film and is connected the gas distributor three in the tail gas oxidation sweetening jar, and tail gas oxidation sweetening tank top connects aiutage through offgas duct behind the oxidation sweetening.
The top of said amine liquid coalescing separator and liquefaction tracheae after the bottom is connected amine wash-out sulphur respectively and amine liquid desolvate and jar manage; Amine liquid coalescing separator separates back liquefaction tracheae through amine liquid and connects the liquefied gas fine filter; The liquefied gas fine filter other end connects one-level liquid film sweetening reaction device through filtering back liquefaction tracheae; One-level liquid film sweetening reaction device top connects first grade desulfurizing alcoholic lye pipe through flange; The other end of first grade desulfurizing alcoholic lye pipe connects the port of export of NaOH solution circulating pump, and the arrival end of NaOH solution circulating pump connects secondary removal of mercaptans knockout drum through alkali liquor pipe behind the secondary removal of mercaptans.
Said liquid film washing contactor is connected the washing circulating pump through water inlet cleaning of evaporator desalination water pipe with washing back desalination water pipe respectively with the washing knockout drum; The tank deck of washing knockout drum is connected with washing back liquefaction tracheae; Be connected with fresh desalination water pipe on the said water inlet cleaning of evaporator desalination water pipe; The fresh desalination water pipe other end connects demineralized water delivery side of pump end, and the entrance point of desalination water pump is connected with fresh demineralized water motion device pipe, is connected with the alkaline sewage pipe after the said washing on the desalination water pipe.
Be provided with zoneofoxidation and disulphide Disengagement zone in the said oxidation knockout tower; Be provided with gas distributor four in the said zoneofoxidation; Gas distributor four-way peroxidating airduct connects the port of export of air cleaner; The arrival end of air cleaner connects the non-purification airduct of pipe network, and said disulphide Disengagement zone connects the disulphide jar through the curing property management, and the bottom of disulphide jar connects disulphide and goes out the device pipe.
Said first grade desulfurizing alcohol knockout drum bottom is connected with rich alkali liquor pipe through flange, and spent lye goes out device Guan Yufu alkali liquor pipe and is interconnected, and the rich alkali liquor pipe other end connects the alkali lye heat exchanger, the alkali lye heat exchanger through heat exchange after the zoneofoxidation of alkali liquor pipe connection oxidation knockout tower.
Said tail gas washing dealkalize jar, tail gas washing digester, membrane separator separate back curing property management through curing property management after curing property management after the washing dealkalize, the washing desulfurization, film respectively and connect the curing property management, and curing property management and film separate back curing property management connection parallel with one another after curing property management after the washing dealkalize, the washing desulfurization.
Bottom, the disulphide Disengagement zone of said oxidation knockout tower is connected with alkali liquor pipe after the oxidation; Alkali liquor pipe is provided with the catalyst injector after the oxidation; The catalyst injector other end connects the alkali lye stripping tower through air inlet stripper alkali liquor pipe, is provided with gas distributor five in the alkali lye stripping tower, and the gas distributor five-way is crossed gas and carried airduct connection oxidation airduct; The entrance point that the back alkali liquor pipe connects the regeneration lye pump is carried through gas in said alkali lye stripping tower bottom; Gas is carried the back and is connected with fresh alkali liquor pipe on the alkali liquor pipe, and the port of export of said regeneration lye pump connects with said and advances the poor alkali liquor pipe that secondary removal of mercaptans alkali liquor pipe is communicated with, and poor alkali liquor pipe is provided with alkali lye prefilter and alkali lye fine filter; Alkali lye stripping tower top is connected with pipeline, and the other end of this pipeline connects oxic gas and puies forward offgas duct.
The beneficial effect of the utility model is:
1. efficient: adopt two-stage liquid film mass transfer technology and set technique, liquid film mass transfer advanced technology, maturation, product liquefied gas mercaptan removal efficiency reaches more than 95%; Alkali liquor oxidized regeneration efficiency is high, and regeneration alkali lye quality is good, and the alkali lye life cycle can reach 6 months more than-12 months.
2. energy-conservation: regeneration alkali lye does not need the hydrotreatment of solvent extraction and sulfur-bearing solvent; Adopt method Separation and Recovery disulphide such as efficient oxidation, low disturbance, air supporting coalescence; Can be used as the chemical resource utilization, or go hydrogenation plant to be converted into hydrogen sulfide and final Recovered sulphur; Alkali liquor oxidizedly under 40 ℃ of left and right sides conditions, carry out, generally do not need the energy consumption of heating and cooling; Removal of mercaptans alkali lye is little with washing demineralized water circular flow, and the pump energy consumption is low.
3. reduce discharging:
(1) the alkaline residue discharging significantly reduces: regeneration alkali lye quality is good, and the alkaline residue discharge capacity is below 1/2 ~ 1/3 of traditional handicraft.
Adopt amine liquid coalescing separator to remove amine liquid in the material liquid gasification (enrichment hydrogen sulfide), reduce the alkaline residue discharging from the source; Alkali lye adopts the efficient oxidation regeneration technology that contacts entirely behind the removal of mercaptans, and sodium mercaptides oxidation conversion speed is high, can guarantee that naoh concentration maintains high level in system's alkali lye, and the removal of mercaptans stabilised efficiency does not descend; Can effectively separate the disulphide that alkali liquor oxidized process generates, to carry content secretly low for disulphide in the regeneration alkali lye, and regeneration alkali lye quality increases substantially.
(2) alkaline sewage of washing generation significantly reduces: liquefied gas alkali lye entrainment low (need not to wash copper strip test can be qualified) after the liquid film alkali cleaning, washing significantly reduces with demineralized water consumption and alkaline sewage discharging.
4. environmental protection:
(1) three waste discharge significantly reduces.
(2) mercaptan more than 80% finally comes out with liquid disulphide isolated in form in the material liquid gasification, goes the petroleum naphtha hydrogenation device to be converted into hydrogen sulfide, finally is converted into sulphur, also can be used as the industrial chemicals utilization after making with extra care.
(3) alkali liquor oxidized, the gas of design is carried tail gas and is handled through level Four, can disulphide in the tail gas be removed to 1000mg/m 3(0.035%v), this tail gas need not go burning disposal, just can be directly to smoke stack emission, and recyclable disulphide can reduce tail gas on the other hand and burn the pollution of generation sulfur dioxide to atmosphere on the one hand.
5. device operating cost is low: the utility model operating cost (liquefied gas is made with extra care cost) is low, is about 1/4 of traditional handicraft.
Description of drawings
According to accompanying drawing the utility model is done further explain below.
Fig. 1 is the structured flowchart of the combined system of the described a kind of liquid gas sweetening of the utility model embodiment.
Among the figure:
1, amine liquid coalescing separator; 2, one-level liquid film sweetening reaction device; 3, secondary liquid film sweetening reaction device; 4, liquid film washing contactor; 5, oxidation knockout tower; 6, alkali lye stripping tower; 7, disulphide jar; 8, tail gas washing dealkalize jar; 9, tail gas washing digester; 10, membrane separator; 11 and tail gas oxidation sweetening jar; 12, liquefied gas fine filter; 13, first grade desulfurizing alcohol knockout drum; 14, alkali lye heat exchanger; 15, catalyst injector; 16, the tracheae that liquefies behind the first grade desulfurizing alcohol; 17, advance secondary removal of mercaptans alkali liquor pipe; 18, secondary removal of mercaptans knockout drum; 19, the tracheae that liquefies behind the secondary removal of mercaptans; 20, washing knockout drum; 21, oxic gas is put forward offgas duct; 22, gas distributor one; 23, offgas duct after the washing dealkalize; 24, gas distributor two; 25, offgas duct after the washing desulfurization; 26, polymeric membrane; 27, film separates the back offgas duct; 28, gas distributor three; 29, offgas duct behind the oxidation sweetening; 30, aiutage; 31, the tracheae that liquefies behind the amine wash-out sulphur; 32, the amine liquid pipe that desolvates jar; 33, amine liquid separates back liquefaction tracheae; 34, filter back liquefaction tracheae; 35, first grade desulfurizing alcoholic lye pipe; 36, NaOH solution circulating pump; 37, alkali liquor pipe behind the secondary removal of mercaptans; 38, water inlet cleaning of evaporator desalination water pipe; 39, washing back desalination water pipe; 40, washing circulating pump; 41, washing back liquefaction tracheae; 42, fresh desalination water pipe; 43, desalination water pump; 44, fresh demineralized water motion device pipe; 45, alkaline sewage pipe; 46, gas distributor four; 47, oxidation airduct; 48, air cleaner; 49, pipe network comes non-purification airduct; 50, curing property management; 51, disulphide goes out the device pipe; 52, rich alkali liquor pipe; 53, spent lye goes out the device pipe; 54, alkali liquor pipe after the heat exchange; 55, curing property management after the washing dealkalize; 56, curing property management after the washing desulfurization; 57, film separates back curing property management; 58, alkali liquor pipe after the oxidation; 59, air inlet stripper alkali liquor pipe; 60, gas distributor five; 61, gas is carried airduct; 62, gas is carried the back alkali liquor pipe; 63, regeneration lye pump; 64, fresh alkali liquor pipe; 65, poor alkali liquor pipe; 66, alkali lye prefilter; 67, alkali lye fine filter.
The specific embodiment
As shown in Figure 1; The combined system of the described a kind of liquid gas sweetening of the utility model embodiment; Comprise amine liquid coalescing separator 1, one-level liquid film sweetening reaction device 2, secondary liquid film sweetening reaction device 3, liquid film washing contactor 4, oxidation knockout tower 5, alkali lye stripping tower 6, disulphide jar 7, tail gas washing dealkalize jar 8, tail gas washing digester 9, membrane separator 10 and tail gas oxidation sweetening jar 11; Be provided with liquefied gas fine filter 12 between said amine liquid coalescing separator 1 and the one-level liquid film sweetening reaction device 2; One-level liquid film sweetening reaction device 2 bottoms connect first grade desulfurizing alcohol knockout drum 13 through flange; Be provided with alkali lye heat exchanger 14 between first grade desulfurizing alcohol knockout drum 13 and the oxidation knockout tower 5; Be provided with catalyst injector 15 between oxidation knockout tower 5 and the alkali lye stripping tower 6; Said first grade desulfurizing alcohol knockout drum 13 connects secondary liquid film sweetening reaction device 3 through liquefaction tracheae 16 behind the first grade desulfurizing alcohol; Secondary liquid film sweetening reaction device 3 tops are connected with into secondary removal of mercaptans alkali liquor pipe 17; Secondary liquid film sweetening reaction device 3 bottoms connect secondary removal of mercaptans knockout drum 18 through flange, and secondary removal of mercaptans knockout drum 18 connects liquid film washing contactor 4 through liquefaction tracheae 19 behind the secondary removal of mercaptans, and liquid film washing contactor 4 bottoms connect washing knockout drum 20 through flange; Said oxidation knockout tower 5 tops are put forward offgas duct 21 through oxic gas and are connected the gas distributor 1 in the tail gas washing dealkalize jar 8; Tail gas washing dealkalize jar 8 tops through the washing dealkalize after offgas duct 23 connect the gas distributor 2 24 in the tail gas washing digesters 9, tail gas washing digester 9 tops through the washing desulfurization after offgas duct 25 junctional membrane separators 10, be provided with polymeric membrane 26 in the membrane separator 10; Membrane separator 10 tops are separated back offgas duct 27 through film and are connected the gas distributor 3 28 in the tail gas oxidation sweetening jar 11, and tail gas oxidation sweetening jar 11 tops connect aiutage 30 through offgas duct behind the oxidation sweetening 29.
The top of said amine liquid coalescing separator 1 and liquefaction tracheae 31 after the bottom is connected amine wash-out sulphur respectively and the amine liquid jar pipe 32 that desolvates; Amine liquid coalescing separator 1 separates back liquefaction tracheae 33 through amine liquid and connects liquefied gas fine filter 12; Liquefied gas fine filter 12 other ends connect one-level liquid film sweetening reaction device 2 through filtering back liquefaction tracheae 34; One-level liquid film sweetening reaction device 2 tops connect first grade desulfurizing alcoholic lye pipe 35 through flange; The other end of first grade desulfurizing alcoholic lye pipe 35 connects the port of export of NaOH solution circulating pump 36, and the arrival end of NaOH solution circulating pump 36 connects secondary removal of mercaptans knockout drum 18 through alkali liquor pipe behind the secondary removal of mercaptans 37.
Said liquid film washing contactor 4 is connected washing circulating pump 40 through water inlet cleaning of evaporator desalination water pipe 38 with washing back desalination water pipe 39 respectively with washing knockout drum 20; The tank deck of washing knockout drum 20 is connected with washing back liquefaction tracheae 41; Be connected with fresh desalination water pipe 42 on the said water inlet cleaning of evaporator desalination water pipe 38; Fresh desalination water pipe 42 other ends connect the port of export of desalination water pump 43; The entrance point of desalination water pump 43 is connected with fresh demineralized water motion device pipe 44, is connected with alkaline sewage pipe 45 on the said washing back desalination water pipe 39.
Be provided with zoneofoxidation and disulphide Disengagement zone in the said oxidation knockout tower 5; Be provided with gas distributor 4 46 in the said zoneofoxidation; Gas distributor 4 46 connects the port of export of air cleaner 48 through oxidation airduct 47; The arrival end of air cleaner 48 connects the non-purification airduct 49 of pipe network, and said disulphide Disengagement zone connects disulphide jar 7 through curing property management 50, and the bottom of disulphide jar 7 connects disulphide and goes out device pipe 51.
Said first grade desulfurizing alcohol knockout drum 13 bottoms are connected with rich alkali liquor pipe 52 through flange; Spent lye goes out device pipe 53 and is interconnected with rich alkali liquor pipe 52; Rich alkali liquor pipe 52 other ends connect alkali lye heat exchanger 14, and alkali lye heat exchanger 14 connects the zoneofoxidation of oxidation knockout tower 5 through alkali liquor pipe after the heat exchange 54.
Said tail gas is washed dealkalize jar 8, tail gas washing digester 9, membrane separator 10 and is connected curing property managements 50 through curing property management 56 after curing property management 55 after the washing dealkalize, the washing desulfurization, film separation back curing property management 57 respectively, curing property management 56 and curing property management 57 connections parallel with one another of film separation back after curing property management 55 after the washing dealkalize, the washing desulfurization.
Bottom, the disulphide Disengagement zone of said oxidation knockout tower 5 is connected with alkali liquor pipe 58 after the oxidation; Alkali liquor pipe 58 is provided with catalyst injector 15 after the oxidation; Catalyst injector 15 other ends connect alkali lye stripping tower 6 through air inlet stripper alkali liquor pipe 59; Be provided with gas distributor 5 60 in the alkali lye stripping tower 6; Gas distributor 5 60 is carried airduct 61 through gas and is connected oxidation airduct 47, and the entrance point that back alkali liquor pipe 62 connects regeneration lye pump 63 is carried through gas in said alkali lye stripping tower 6 bottoms, and gas is carried on the alkali liquor pipe 62 of back and is connected with fresh alkali liquor pipe 64; The port of export of said regeneration lye pump 64 connects with said and advances the poor alkali liquor pipe 65 that secondary removal of mercaptans alkali liquor pipe 17 is communicated with; Poor alkali liquor pipe 65 is provided with alkali lye prefilter 66 and alkali lye fine filter 67, and alkali lye stripping tower 6 tops are connected with pipeline, and the other end of this pipeline connects oxic gas and puies forward offgas duct 21.
The utility model adopts fiber liquid film mass transfer technology; Utilize surface tension and gravitational field principle, alkali lye is extended on special hydrophilic fibers form the ultra-thin alkali lye liquid film of very big area, liquefied gas passes through between the alkali lye liquid film; Alkali lye and liquefied gas contact area significantly increase; Interphase mass transfer distance shortens greatly, and two contact fully and are swift in response, thereby improves in the liquefied gas reaction depth of NaOH in the mercaptan and alkali lye.The alkaline sewage that washing is produced significantly reduces, liquefied gas alkali lye entrainment low (need not to wash copper strip test can be qualified) after the liquid film alkali cleaning, and washing significantly reduces with demineralized water consumption and alkaline sewage discharging.
Adopt amine liquid coalescing separator that liquefied gas is carried out preliminary treatment, the amine liquid more than 90% is come out by coarse separation, has significantly reduced the alkaline residue discharging that causes because of hydrogen sulfide.During concrete the use, the liquefied gas behind the amine wash-out sulphur removes the amine liquid of carrying secretly in the liquefied gas through amine liquid coalescing separator 1, and the amine liquid of recovery gets into solvent tank.Liquefied gas behind the separation of amine liquid gets into one-level liquid film sweetening reaction device 2 from liquefied gas inlet and alkali lye import respectively with circulation alkali liquor, and accomplishes elementary removal of mercaptans after liquefied gas fine filter 12 filters.The sedimentation separation in knockout drum of liquefied gas and alkali lye, liquefied gas goes out from tank deck subsequently, gets into secondary liquid film sweetening reaction device 3 from liquefied gas inlet and alkali lye import respectively with regeneration alkali lye, and accomplishes the secondary removal of mercaptans.Liquefied gas and alkali lye are in the knockout drum sedimentation separation, and liquefied gas goes out from tank deck at any time.Regeneration alkali lye is sent here by regeneration lye pump 63, passes through alkali lye prefilter 66 and alkali lye fine filter 67 double-filtrations successively, sends to the secondary removal of mercaptans.Alkali lye behind the secondary removal of mercaptans is sent to removal of mercaptans by NaOH solution circulating pump 36, and the rich alkali lye behind the first grade desulfurizing alcohol gets into alkali liquor oxidized knockout tower 5 through rich alkali liquor pipe 52.
Demineralized water forms liquid film in special hydrophilic filler, form the ultra-thin moisture film of very big area, and liquefied gas passes through from intermembranous; Two areas that contact are very big; The mass transfer distance of moisture film is extremely short, and the alkaline plasma that liquefied gas is carried secretly (polarity ion) is extracted in the demineralized water, accomplishes washing and removes the alkali process.Under density contrast, gravity, hydrophilic fibers coalescence and the effect of fluid motive force, demineralized water is settled down to knockout drum and separates fast with liquefied gas along fiber.
Liquefied gas gets into from liquid film washing contactor 4 tops with the demineralized water of being sent here by washing circulating pump 40 behind the removal of mercaptans, and in liquid film washing contactor 4, accomplishes the washing dealkalize.Liquefied gas separates at washing knockout drum 20 with demineralized water after the dealkalize, and liquefied refinery gas goes out device; The demineralized water circulation is used for dealkalize, and according to product liquefied gas sodium ions content rising situation periodic replacement demineralized water, fresh demineralized water is sent here by fresh desalination water pump 43.
Alkali liquor oxidized regeneration belongs to the gas-liquid two-phase reaction, and the principal element that influences reaction rate is the contact area of gas-liquid two phases.The utility model adopts gas distributor that oxidation air is dispersed in the alkali lye with the microvesicle form; Air becomes the order of magnitude to increase with the alkali lye contact area; Significantly improved the oxidation conversion speed of sodium mercaptides in the alkali lye; Alkali liquor oxidized efficient improves 2-3 doubly than traditional handicraft, after the oxidation in the alkali lye sodium mercaptides concentration can be stabilized in below the 1%wt.Alkali liquor oxidized regeneration efficiency is high, and regeneration alkali lye quality is good, and the alkali lye life cycle can reach 6 months more than-12 months.Simultaneously; Under efficient oxidation tower structure condition; Because disturbance is little in air and the alkaline reaction process, sodium mercaptides oxidation conversion speed is fast, the disulphide of the big drop of the disulphide of generation coalescence under microvesicle air supporting effect formation has been avoided the emulsification of disulphide in regeneration alkali lye; The 30-100 that the disulphide mean drop diameter is about conventional filler tower oxidation technology doubly very helps separating of disulphide and alkali lye.Disulphide more than 80% is separated (other part is mainly taken away with the tail gas volatilization) with liquid form; Disulphide content drops to below the 500ppm in the regeneration alkali lye; Can produce the product liquefied gas hardly when this alkali lye circulation is used for liquid gas sweetening and add the sulphur effect; Therefore do not need frequent change alkali lye, just can control product liquefied gas total sulfur and reach design objective.
Two districts (alkali liquor oxidized district and disulphide Disengagement zone) about alkali liquor oxidized knockout tower 5 is divided into by dividing plate.Rich alkali lye behind the removal of mercaptans gets into zoneofoxidation from the 5 bottom alkali lye imports of oxidation knockout tower; Compressed air gets into from the 5 bottom zoneofoxidation imports of oxidation knockout tower after air cleaner 48 filters; Gas distributor 4 46 in peroxidating knockout tower 5 is dispersed in the alkali lye in the oxidation knockout tower 5 with the microvesicle form, and alkali lye fully contacts and accomplishes mercaptan oxidation and transforms with air.If alkali liquid temperature is lower than 30 ℃, utilize alkali lye heat exchanger 14 to be heated to 30-45 ℃.Alkali lye and tail gas separate at oxidation knockout tower 5 cats head fast after the oxidation; Excessive peroxidating knockout tower 5 Internal baffles of alkali lye after the oxidation get into the disulphide Disengagement zone; The disulphide that generates is from phase coalescence, because density is little and the polarity difference floats on the alkali lye, alkali lye is deposited in lower floor.Fresh alkali lye utilization regeneration lye pump 63 is sent into this device.Alkaline residue can directly discharge through alkali liquor pipe 37 behind the removal of mercaptans, or is disposed to the alkaline residue jar through regeneration lye pump 63.Alkali liquor oxidized with catalyst through being arranged on catalyst injector 15 regular replenishment on the alkali liquor pipe 58 after the oxidation.
Alkali lye comes out from the bottom, Disengagement zone after separating disulphide; And get into from the alkali lye import of alkali lye stripping tower 6; Air after air cleaner SR005 filters is scattered in the alkali lye with microvesicle through the gas distributor 5 60 in the alkali lye stripping tower 6; Two fully contacts mutually, the disulphide of trace is dissolved in the air and is brought in the tail gas in the alkali lye.Tail gas is discharged from alkali lye stripping tower 6 tops of tower, and alkali lye is being discharged at the bottom of alkali lye stripping tower 6 towers behind the alkali lye stripping tower 6 tower bottom standing separation gases, sends to the liquid gas sweetening unit through regeneration lye pump 63.
Oxidation and gas are carried back tail gas through the 8 washing dealkalizes of tail gas washing dealkalize jar, are scattered in the water in the washing dealkalize jar 8 with the microvesicle form through gas distributor 1, can remove the gentle micro-alkali lye of carrying secretly in the tail gas of carrying of alkali liquor oxidized regeneration by water elution; Again through the 9 washing desulfurization of tail gas washing digester; Be scattered in the washing digester 9 interior water with the microvesicle form through gas distributor 2 24; Tail gas fully contacts with water; Part disulphide in the tail gas is prone to be condensed in the water by washing because boiling point is low, because promptly poor washing digester 9 bottoms that fall to of density; The small drop of disulphide poling after the washing desulfurization in the tail gas; Through membrane separator 10 time, utilize the microporous barrier double-thinning property, fine droplet shape disulphide is tackled; And gas is passed through, wherein separated liquid disulphide major part is compiled in pot bottom; Microporous barrier separates back tail gas and is dispersed in the oxidant with the microvesicle form through gas distributor 3 28 effect backs, residual disulphide is oxidized to salt is dissolved in the oxidant.That the utility model also is designed with is alkali liquor oxidized, gas is carried tail gas and handled through level Four, can disulphide in the tail gas be removed to 1000mg/m 3(0.035%v), this tail gas need not go burning disposal, just can be directly to smoke stack emission, and recyclable disulphide can reduce tail gas on the other hand and burn the pollution of generation sulfur dioxide to atmosphere on the one hand.The disulphide that reclaims mixes in the gasoline, goes hydrogenation plant to be converted into hydrogen sulfide, final production sulphur, or recycle by producer.
Adopt amine liquid coarse separation, two-stage liquid film removal of mercaptans, the dealkalize of washing liquid film, alkali liquor efficient oxidation regeneration technology, alkali lye gas to propose technology, the combination of tail gas desulphurization system; Make and alkali liquor oxidizedly under 40 ℃ of left and right sides conditions, carry out; The general energy consumption that does not need heating and cooling, removal of mercaptans alkali lye is little with washing demineralized water circular flow, and the pump energy consumption is low; Device operating cost (liquefied gas is made with extra care cost) is low, is about 1/4 of traditional handicraft.
The utility model is not limited to above-mentioned preferred forms; Anyone can draw other various forms of products under the enlightenment of the utility model; No matter but on its shape or structure, do any variation; Every have identical with a application or akin technical scheme, all drops within the protection domain of the utility model.
Claims (7)
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| CN2012200126538U CN202446974U (en) | 2012-01-12 | 2012-01-12 | Combination system for removing mercaptan from liquefied gas |
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| CN103805274A (en) * | 2014-03-04 | 2014-05-21 | 中国石油化工股份有限公司 | Liquefied gas desulfurization refining device and liquefied gas desulfurization refining method in oil refinery |
| CN104371759A (en) * | 2013-08-14 | 2015-02-25 | 宁波北仑千和环保工程有限公司 | Comprehensive utilization apparatus of waste mineral oil |
| CN104789262A (en) * | 2015-04-22 | 2015-07-22 | 宁波中一石化科技股份有限公司 | Complete set of energy conservation and emission reduction type device and method for desulfurization and three-waste treatment of oil refinery |
| CN105112092A (en) * | 2015-08-24 | 2015-12-02 | 宁波中一石化科技股份有限公司 | Reverse extraction device and method for gas condensate fiber liquid membrane sulfur and alcohol removing and alkali liquor regeneration solvent |
| CN107227173A (en) * | 2016-03-25 | 2017-10-03 | 中国石油化工股份有限公司 | The combination unit of catalytic liquefaction gas deep desulfuration |
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2012
- 2012-01-12 CN CN2012200126538U patent/CN202446974U/en active IP Right Grant
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104371759A (en) * | 2013-08-14 | 2015-02-25 | 宁波北仑千和环保工程有限公司 | Comprehensive utilization apparatus of waste mineral oil |
| CN103571524A (en) * | 2013-12-06 | 2014-02-12 | 宁波中一石化科技有限公司 | Device and method for removing cracking C5 total sulfur |
| CN103571524B (en) * | 2013-12-06 | 2016-04-27 | 宁波中一石化科技有限公司 | Remove cracking c_5 total sulfur apparatus and method |
| CN103805274A (en) * | 2014-03-04 | 2014-05-21 | 中国石油化工股份有限公司 | Liquefied gas desulfurization refining device and liquefied gas desulfurization refining method in oil refinery |
| CN103805274B (en) * | 2014-03-04 | 2016-07-13 | 中国石油化工股份有限公司 | A kind of device and method of oil refinery liquefied gas desulfuration purification |
| CN104789262A (en) * | 2015-04-22 | 2015-07-22 | 宁波中一石化科技股份有限公司 | Complete set of energy conservation and emission reduction type device and method for desulfurization and three-waste treatment of oil refinery |
| CN105112092A (en) * | 2015-08-24 | 2015-12-02 | 宁波中一石化科技股份有限公司 | Reverse extraction device and method for gas condensate fiber liquid membrane sulfur and alcohol removing and alkali liquor regeneration solvent |
| CN107227173A (en) * | 2016-03-25 | 2017-10-03 | 中国石油化工股份有限公司 | The combination unit of catalytic liquefaction gas deep desulfuration |
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Address after: 315040, Zhejiang, Ningbo province National hi tech Zone Lingyun road 1177 Lingyun Industrial Park, building 10, north 2 floor Patentee after: Ningbo Zhongyi Petrochemical Technology Co., Ltd. Address before: 1618, room 1558, 315040 Jiangnan Road, Ningbo science and Technology Park, Zhejiang, China Patentee before: Ningbo Zhongyi Petrochemical Technology Co., Ltd. |
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Address after: 315040, Zhejiang, Ningbo province National hi tech Zone Lingyun road 1177 Lingyun Industrial Park, building 10, north 2 floor Patentee after: NINGBO ZHONGYI PETROCHEMICAL TECHNOLOGY CO., LTD. Address before: 315040, Zhejiang, Ningbo province National hi tech Zone Lingyun road 1177 Lingyun Industrial Park, building 10, north 2 floor Patentee before: Ningbo Zhongyi Petrochemical Technology Co., Ltd. |
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