CN105195018A - Method for reducing loss of liquefied gas in desulfurization process - Google Patents
Method for reducing loss of liquefied gas in desulfurization process Download PDFInfo
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- CN105195018A CN105195018A CN201510689870.9A CN201510689870A CN105195018A CN 105195018 A CN105195018 A CN 105195018A CN 201510689870 A CN201510689870 A CN 201510689870A CN 105195018 A CN105195018 A CN 105195018A
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Abstract
The invention relates to a method for reducing the loss of liquefied gas in a desulfurization process. The method comprises the following steps: the liquefied gas enters from the bottom of a desulfurization tower to be in reversed contact absorption with amine liquid entering from the top of the tower; the amine liquid in the desulfurized liquefied gas is removed and recycled back to the tower through a separation module arranged at the top of the tower; the amine carrying amount of the liquefied gas is reduced to be lower than 20mg/L from 100mg/L to 1000mg/L. The liquefied gas in a bottom pregnant solution is separated and recycled by setting a two-section type rapid deep separation module: a first-section module is a primary-grade rapid separation module arranged at the bottom of the tower; the carrying amount of the liquefied gas is rapidly reduced to be no more than 100mg/L from 1000mg/L to 5000mg/L; a second-section module is a deep separation tank which is arranged between an amine liquid outlet at the bottom of the tower and a flash tank, and the carrying amount of the liquefied gas in the pregnant solution is then reduced to be no more than 15mg/L; the separated liquefied gas and the liquefied gas at the top of the desulfurization tower are discharged together, and the amine liquid enters the flash tank after the treatment. The method is rapid in treatment speed and high in efficiency; the spaces of the tower top and the tower bottom of the desulfurization tower are effectively utilized and the cost is greatly reduced.
Description
Technical field
The present invention relates to a kind of method reducing liquefied gas loss in sweetening process, specifically, fast deep separation module is adopted to isolate the liquid hydrocarbon carried secretly in amine liquid, reduce the loss of removing liquefied gas in flash tank amine liquid, isolate the amine liquid that tower top liquefied gas is carried secretly simultaneously, reduce the use of External liquefying qi exhaustion amine equipment.
Background technology
Generally have liquefied gas (also claiming liquefied petroleum gas, LGP) product to generate in petroleum refining process, its ratio accounts for 4 ~ 8%wt of crude oil total amount.Liquefied gas is primarily of productions such as refinery catalytic cracking unit, coking plant, atmospheric and vacuum distillation unit, reformer, light ends units, its key component is carbon three, C_4 hydrocarbon, containing a small amount of carbon two, carbon five hydro carbons, also containing hydrogen sulfide (about 0.01 ~ 4%), mercaptan (about 1 ~ 9000mg/m
3), thioether (0 ~ 100mg/m
3), COS sulfides.Refinery's liquefied gas because of its source different with component, each sulfide content difference is very large, but is mainly hydrogen sulfide and mercaptan, and their existence not only can cause product quality to decline, have a strong impact on its serviceability, as the environmental pollution etc. that conveying and storage process bring burn into combustion process to bring.Especially, as catalytic cracking and the coking liquefied gas of petrochemical process (as MTBE production, alkylation process and polypropylene process etc.) raw material, if the too high meeting of sulfur content causes the degradation of catalysqt deactivation and product quality.Therefore, must be removed before each machining cell.
The refinery gas such as catalytic cracked dry gas, liquefied gas sulfur removal technology is generally divided into two large classes: dry desulfurization, and being mainly used in need compared with the occasion of high desulfurization rate, conventional zinc oxide method, active carbon adsorption; Wet desulphurizations etc., wherein the most generally use alcohol amine desulfurization.Alcohol amine desulfurization is a kind of typical absorption-regenerative response process, and its typical reaction process is as follows:
To hydrogen sulfide:
Above-mentioned reaction is reversible reaction, at a lower temperature (25 ~ 40 DEG C), and reaction is carried out (absorption) left.(be greater than 105 DEG C) at relatively high temperatures, reaction is carried out (desorb) to the right, and the sulfide of the amine now generated decomposes, and separate out hydrogen sulfide, alcohol amine solvent is reproduced, and can recycle.
Domestic certain petro-chemical corporation liquid hydrocarbon desulfurization tower T3201 is liquid/liquid extraction tower, and this tower is gently liquefied petroleum gas mutually, and heavy phase is the MDEA cleaning solution of 30%.Former design liquid hydrocarbon 16.8 ten thousand tons/year, namely liquid hydrocarbon flow is 21t/h, and lean solution amount is 28t/h.At present because liquid hydrocarbon sulfur content is low, lean solution amount reduces to 9t/h, and after de-, liquid hydrocarbon is up-to-standard; But liquid hydrocarbon amount reaches 40t/h, often there is rich solution band hydrocarbon phenomenon.
The main cause of this problem is caused to be change due to weight phase volume flow proportional, former design weight phase volume flow-rate ratio is about 1.3:1, and operate operating mode lower volume ratio at present and be about 2.5:1, this tower up flow velocity in running increases, because the sedimentation separation space of tower top and the bottom design does not become, therefore top liquid hydrocarbon band amine liquid and bottom amine liquid band liquid hydrocarbon is caused, and increase due to the ratio of liquid hydrocarbon, therefore the situation of liquid hydrocarbon band amine liquid is not serious relatively, and the problem of amine liquid band liquid hydrocarbon can be relatively outstanding.
All pass through the method increasing tower base space at present, namely improve the rich solution time of staying, and then control the entrainment of liquefied gas in rich solution.
Summary of the invention
The invention provides a kind of method reducing liquefied gas loss in sweetening process, the operating procedure of described method comprises liquefied gas and absorbs by entering reverse contact of the amine liquid entered with top of tower bottom desulfurizing tower, the amine liquid carried secretly in liquefied gas after desulfurization is removed and is recovered in tower by the separation module arranged by tower top, and liquefaction band of gas amine amount is reduced to from 100 ~ 1000mg/L and is less than 20mg/L.By arranging two-part fast deep separation module, separation and recovery is carried out to the liquefied gas that end rich solution is carried secretly: first paragraph module is the elementary quick separating module be arranged at the bottom of tower, and liquefied gas entrainment is reduced within 100mg/L fast from 1000 ~ 5000mg/L; Second segment is arranged on the degree of depth knockout drum at the bottom of tower between the outlet of amine liquid and flash tank, and in rich solution, liquefied gas entrainment is reduced within 15mg/L again; Isolated liquefied gas and desulfurization tower top liquefied gas are together discharged, and after process, amine liquid removes flash tank.
Concrete technical scheme of the present invention is as follows:
Reduce a device for liquefied gas loss in sweetening process, described device comprises liquefaction qi exhaustion amine unit, elementary quick separating unit, the outlet of amine liquid and degree of depth separation equipment;
Described liquefaction qi exhaustion amine unit is arranged on desulfurizing tower tower top, and thickness is 100mm to 400mm, determines according to the height of amine liquid entrainment, and the upper cover of itself and desulfurizing tower is at a distance of 100 ~ 600mm;
Described elementary quick separating unit is arranged at the bottom of desulfurizing tower tower, and thickness is 100mm to 600mm, determines according to the height of amine liquid entrainment, and the low head of itself and desulfurizing tower is at a distance of 100 ~ 600mm;
Described amine liquid outlet is arranged at the bottom of desulfurizing tower tower, is connected, establishes degree of depth separative element in described degree of depth separation equipment by flash tank with described degree of depth separation equipment.
Described liquefaction qi exhaustion amine unit is level or vertical setting, comprises the coalescent module of coarse and nona modified fiber module.
Described elementary quick separating unit is level or vertical setting, comprises the coalescent module of coarse and nona modified fiber pre-separation module.
Described degree of depth separative element is vertical setting, comprises nona modified fiber degree of depth separation module and modification ripple strengthening settling module.
Described desulfurizing tower is respectively arranged with interfacial meter at the bottom of tower top interfacial meter and tower at the bottom of tower top and tower; The upper and lower side of described tower top interfacial meter is connected in liquefied gas, and at the bottom of described tower, the upper and lower side of interfacial meter is connected in amine liquid.
When described elementary quick separating unit is vertical setting, arrange floating passage at the nona modified fiber pre-separation module rear of amine liquid flow direction, the diameter of described floating passage is 15 ~ 20mm.
Utilize above-mentioned arbitrary device to carry out the method for desulfurization, comprise the steps:
In desulfurizing tower, input liquefied gas, liquefied gas removes by described liquefaction qi exhaustion amine unit the amine liquid carried secretly in liquefied gas; Described liquefied gas is 0.01 ~ 0.02m/s through each module flow velocity upwards, the coalescent module pressure drop of coarse of described liquefaction qi exhaustion amine unit within 0.005MPa, the pressure drop of nona modified fiber module is 0.005 ~ 0.01MPa, coalescent amine liquid size droplet diameter of growing up is 30 ~ 50 μm; Within after the process of described liquefaction qi exhaustion amine unit, the band amine liquid measure of liquefied gas is reduced to 20mg/L from 100 ~ 1000mg/L;
Described elementary quick separating unit removes the liquefied gas carried secretly in rich solution, the coalescent module pressure drop of coarse of described elementary quick separating unit within 0.005MPa, the pressure drop of nona modified fiber pre-separation module is 0.005 ~ 0.01MPa, coalescent oil droplet size of growing up is 30 ~ 50 μm; Flow through the flow control of the rich solution of each module at 0.015 ~ 0.025m/s; Remove rear described liquefied gas entrainment to be reduced to fast within 100mg/L from 1000 ~ 5000mg/L;
The flow control of rich solution in described degree of depth separation equipment is 0.015 ~ 0.025m/s, and liquefied gas entrainment is reduced within 15mg/L fast from 50 ~ 100mg/L.
The isolated liquefied gas of the degree of depth is discharged by degree of depth separation equipment top oil bag and is removed follow up device in the lump with desulfurizing tower top liquefied gas, and after being separated, amine liquid removes subsequent production device again through flash tank.
The pressure of described desulfurizing tower is 0.6 ~ 5Mpa, and temperature is 30 ~ 70 DEG C.
At liquefaction qi exhaustion amine unit when for vertical setting; at the two blocks of arc column plates that are crisscross arranged apart from upper cover 100mm position; distance between plates 300 ~ 500mm; module is vertically arranged between two blocks of arc column plates; size and two arc column plate snug fit; thickness is 100mm to 400mm according to the height of amine liquid entrainment; between the vertical two arc column plates arranging de-amine unit, flow velocity is at 0.01 ~ 0.02m/s; the coalescent module pressure drop of coarse is within 0.005MPa, and the pressure drop of nona modified fiber module is 0.005 ~ 0.01Mpa.
Wherein, tower top takes off the coalescent module of coarse in amine unit and nona modified fiber module all adopts hydrophilic oleophobic material.
When being horizontally disposed with liquefaction qi exhaustion amine unit, tower top interfacial meter two interface is all arranged on below de-amine unit, it is vertical when de-amine unit is set, tower top interfacial meter two interface is all arranged on de-amine unit liquefied gas and flows into side, two kinds arrange and all go up end interface and be connected in liquefied gas, lower end interface is connected in amine liquid, and control liquefied gas and amine liquid interface are in the middle of two interfaces.
When described elementary quick separating unit is vertical setting, at the two blocks of arc column plates that are crisscross arranged apart from low head 100mm position, distance between plates 300 ~ 500mm, module is vertically arranged between two blocks of arc column plates, size and two arc column plate snug fit, thickness is 100mm to 600mm according to the height of amine liquid entrainment, at amine liquid flow direction fibre module rear, floating passage is set, diameter is at 15 ~ 20mm, between the vertical two arc column plates arranging the coalescent module of coarse, flow velocity is at 0.015 ~ 0.025m/s, the coalescent module pressure drop of coarse is within 0.005MPa, the pressure drop of nona modified fiber pre-separation module is 0.005 ~ 0.01Mpa.
Wherein, in elementary quick separating unit at the bottom of tower, the coalescent module of coarse and nona modified fiber quick separating module all adopt lipophilic-hydrophobic property material.
When being horizontally disposed with elementary quick separating unit, interfacial meter two interface at the bottom of tower is all arranged on above elementary quick separating unit, it is vertical when de-amine unit is set, interfacial meter two interface at the bottom of tower is all arranged on elementary quick separating unit amine liquid and flows into side, two kinds arrange and all go up end interface and be connected in liquefied gas, lower end interface is connected in amine liquid, and control liquefied gas and amine liquid interface are in the middle of two interfaces.
Compared with prior art, the present invention has following advantage:
(1) traditional desulfurizing tower amine liquid carries liquefied gas content secretly is 3000 ~ 5000mg/L, and in method amine liquid provided by the invention, liquefied gas is separated fast, and efficiency is high, and after being separated, in amine liquid, liquefied gas content is less than 15mg/L, and removal efficiency is higher than 99%;
(2) simply, pressure drop is little, can select installation form and block combiner mode, strong adaptability according to technical indicator for technical process principle and flow process;
(3) effectively make use of the tower top tower base space of desulfurizing tower, greatly reduce costs.
Accompanying drawing explanation
Fig. 1 is the apparatus structure schematic diagram of embodiment 1;
Fig. 2 be tower top take off amine unit be horizontally disposed with pattern;
Fig. 3 is that tower top takes off the vertical of amine unit and arranges pattern;
Fig. 4 be elementary quick separating unit at the bottom of tower be horizontally disposed with pattern;
Fig. 5 is that at the bottom of tower, elementary the vertical of quick separating unit arranges pattern;
Fig. 6 is the structural representation that the degree of depth takes off liquefied gas knockout drum.
Symbol description:
1 desulfurizing tower; 2 degree of depth take off liquefied gas knockout drum; 3 flash tanks;
The coalescent module of 4 coarse; 5 nona modified fiber modules;
6 arc column plates; 7 tower top interfacial meters; 8 nano modification quick separating modules;
9 floating passages; Interfacial meter at the bottom of 10 towers; 11 nano modification degree of depth separation modules;
12 modification ripple strengthening settling modules; 13 oil bags.
Detailed description of the invention
Below, by embodiment, the present invention is specifically described.What be necessary to herein means out is; following examples are only for the invention will be further described; can not limiting the scope of the invention be interpreted as, some nonessential improvement and adjustment that professional and technical personnel's content according to the present invention in this field is made, still belong to protection scope of the present invention.
Embodiment 1
Fig. 1 shows a kind of apparatus structure schematic diagram reducing liquefied gas loss in sweetening process, comprises de-amine unit, elementary quick separating unit, the outlet of amine liquid and degree of depth separation equipment.De-amine unit is arranged on the tower top of desulfurizing tower 1, and thickness is 100mm to 400mm, determines according to the height of amine liquid entrainment, and the upper cover of itself and desulfurizing tower 1 is at a distance of 100 ~ 600mm; Elementary quick separating unit is arranged at the bottom of the tower of desulfurizing tower 1, and thickness is 100mm to 600mm, determines according to the height of amine liquid entrainment, and the low head of itself and desulfurizing tower is at a distance of 100 ~ 600mm; The outlet of amine liquid is arranged at the bottom of the tower of desulfurizing tower 1, is connected, establishes the degree of depth to take off liquefied gas knockout drum 2 in degree of depth separation equipment by flash tank 3 with degree of depth separation equipment.
De-amine unit is level or vertical setting, respectively as shown in Figures 2 and 3.
Elementary quick separating unit is level or vertical setting, respectively as shown in Figure 4 and Figure 5.
The degree of depth takes off liquefied gas knockout drum 2 for vertical setting, comprises nona modified fiber degree of depth separation module and modification ripple strengthening settling module, as shown in Figure 6.
Desulfurizing tower 1 is respectively arranged with interfacial meter 10 at the bottom of tower top interfacial meter 7 and tower at the bottom of tower top and tower, and the upper and lower side of tower top interfacial meter 7 is connected in liquefied gas, and at the bottom of tower, the upper and lower side of interfacial meter 10 is connected in amine liquid.
When elementary quick separating unit is vertical setting, arrange floating passage at the nona modified fiber pre-separation module rear of amine liquid flow direction, the diameter of floating passage is 15 ~ 20mm.
Said apparatus is utilized to carry out the specific works process of desulfurization as follows:
First, liquefied gas absorbs by entering reverse contact of the amine liquid entered with top of tower bottom desulfurizing tower 1, the amine liquid that liquefied gas after desulfurization is carried secretly by the de-amine unit arranged by tower top removes and is recovered in tower, wherein, tower top takes off amine unit and comprises the coalescent module 4 of coarse and nona modified fiber module 5, amine liquid drop is grown up through the coalescent module of coarse 4 is coalescent, and the drop of growing up to complete with liquefied gas through nona modified fiber module 5 and is separated, amine liquid with micro-liquefied gas is through being arranged on the elementary quick separating unit of tower bottom, wherein, elementary quick separating unit comprises the coalescent module 4 of coarse and nano modification pre-separation module 8, liquefied gas oil droplet is grown up through the coalescent module of coarse 4 is coalescent, the part oil droplet of growing up to complete with amine liquid through nano modification pre-separation module 8 and is separated, the amine liquid carrying micro-liquefied gas secretly completes the degree of depth through the nano modification degree of depth separation module 11 that the degree of depth takes off in liquefied gas knockout drum 2 and is separated, liquefied gas after separation and the rapid subsidence layering after ripple strengthening settling module 12 of amine liquid, upper strata liquefied gas is derived to derive together with desulfurizing tower 1 tower top liquefied gas product after being full of knockout drum tank deck oil bag 13 and is for further processing, lower floor's amine liquid removes flash tank 3, remain in amine liquid liquefied gas steam carry out burning process, regenerated amine liquid is recycled.
In certain petro-chemical corporation's liquid hydrocarbon desulfurization tower process domestic, have employed the method for liquefied gas loss in reduction sweetening process of the present invention, reduce amine liquid band hydrocarbon phenomenon and liquid hydrocarbon band amine phenomenon.When not adopting method of the present invention, tower top liquefied gas outlet band amine amount is about 500mg/L, and before removing flash tank, amine liquid band hydrocarbon amount is about 3500mg/L, and the operating temperature of experiment is about 30 ~ 70 DEG C, require that de-rear amine liquid band hydrocarbon amount is less than 15mg/L, tower top liquefaction band of gas amine amount is less than 20mg/L.
Scheme Choice: in this programme amine liquid containing liquefied gas content and liquefaction band of gas amine amount all higher, and amine liquid require to remove flash tank before amine liquid band hydrocarbon amount be less than 15mg/L, tower top liquefaction band of gas amine amount is less than 20mg/L.Therefore the vertical de-amine unit that the coalescent module of coarse and nona modified fiber module composition are set of tower top is selected; Two-part is selected to be separated at the bottom of tower; first paragraph adopts the elementary quick separating unit arranging the coalescent module of coarse and nano modification quick separating module composition at the bottom of tower; elementary quick separating unit adopts vertical setting; second segment arranges the degree of depth and takes off liquefied gas knockout drum to complete degree of depth separation, the interior degree of depth separative element be made up of nona modified fiber degree of depth separation module and ripple strengthening settling module.
The coalescent module of described coarse is corrugated board structures; wherein the spacing of corrugated plating is 5 ~ 20mm; trough place has the circular hole of diameter 5 ~ 10mm; spacing between described circular hole is 50 ~ 250mm; the hydrophilic oleophobic material of the coalescent model choice of tower top coarse, the coalescent model choice lipophilic-hydrophobic property of coarse at the bottom of tower material.
Described nona modified fiber module, nano modification pre-separation module and nano modification degree of depth separation module all adopt Ω shape weaving method to weave and form, very large specific area can be provided, greatly improve the degree of purity of water-oil separating, fiber surface is through modification, fiber surface and droplets contact angle are increased to 150 ° by 120 °, fiber surface and water droplet contact angle are reduced to 45 ° by 70 °, through research find lipophilic-hydrophobic property fiber and droplets contact angle larger, oil droplet loading process is longer, more easily separated, otherwise, less with water droplet contact angle, water droplet loading process is also longer, oil-water separation is better.
Described nona modified fiber module adopts Ω shape weaving method, and specific area is 20063m
2/ m
3, permeability is 0.2070 × 10
-9m
2; Described nona modified fiber pre-separation module adopts Ω shape weaving method, and specific area is 9747m
2/ m
3, permeability is 3.1383 × 10
-9m
2; Described nona modified fiber degree of depth separation module also adopts Ω shape weaving method, and specific area is 13848m
2/ m
3, permeability is 0.5799 × 10
-9m
2, show that liquid stream is when fibre module after deliberation, fibre module is drop coalescently provides very large specific area, drop in liquid is continuous collision coalescence in described micro-module, and realize the meticulous separation of drop, specific area is larger, permeability is lower, then oil-water separation is better.
Described modification ripple strengthening settling module adopts the ripple flap of surface modification, Material selec-tion lipophilic-hydrophobic property material, corrugated plating spacing 5 ~ 20mm, sine wave type flowing adds the collision probability of drop, crest place opens and rises floating hole, oil droplet collects in crest summit floating layer by layer, this process separable go out the drop of particle diameter more than 30 μm.The material of normal use has polypropylene, polytetrafluoroethylene (PTFE), stainless steel etc., then through special surface treatment, has good lipophilic-hydrophobic property, acid and alkali-resistance, high temperature resistant, and has good mechanical strength and service life.
Separating resulting: tower top liquefied gas outlet band hydrocarbon amount is at 15mg/L, and tower bottom outlet amine liquid band hydrocarbon amount is 40 ~ 90mg/L, and before removing flash tank, amine liquid band hydrocarbon amount is about 10mg/L, the stable separation requirement being less than 15mg/L.
Claims (8)
1. reduce a device for liquefied gas loss in sweetening process, it is characterized in that, described device comprises liquefaction qi exhaustion amine unit, elementary quick separating unit, the outlet of amine liquid and degree of depth separation equipment;
Described liquefaction qi exhaustion amine unit is arranged on desulfurizing tower tower top, and thickness is 100mm to 400mm, and the upper cover of itself and desulfurizing tower is at a distance of 100 ~ 600mm;
Described elementary quick separating unit is arranged at the bottom of desulfurizing tower tower, and thickness is 100mm to 600mm, and the low head of itself and desulfurizing tower is at a distance of 100 ~ 600mm;
Described amine liquid outlet is arranged at the bottom of desulfurizing tower tower, is connected, establishes degree of depth separative element in described degree of depth separation equipment by flash tank with described degree of depth separation equipment.
2. device according to claim 1, is characterized in that, described liquefaction qi exhaustion amine unit is level or vertical setting, comprises the coalescent module of coarse and nona modified fiber module.
3. device according to claim 1, is characterized in that, described elementary quick separating unit is level or vertical setting, comprises the coalescent module of coarse and nona modified fiber pre-separation module.
4. device according to claim 1, is characterized in that, described degree of depth separative element is vertical setting, comprises nona modified fiber degree of depth separation module and modification ripple strengthening settling module.
5. device according to claim 1, it is characterized in that, described desulfurizing tower is respectively arranged with interfacial meter at the bottom of tower top interfacial meter and tower at the bottom of tower top and tower, and the upper and lower side of described tower top interfacial meter is connected in liquefied gas, and at the bottom of described tower, the upper and lower side of interfacial meter is connected in amine liquid.
6. device according to claim 3, is characterized in that, when described elementary quick separating unit is vertical setting, arrange floating passage at the nona modified fiber pre-separation module rear of amine liquid flow direction, the diameter of described floating passage is 15 ~ 20mm.
7. utilize the arbitrary described device of claim 1 to 6 to carry out the method for desulfurization, it is characterized in that, comprise the steps:
In desulfurizing tower, input liquefied gas, liquefied gas removes by described liquefaction qi exhaustion amine unit the amine liquid carried secretly in liquefied gas; Described liquefied gas is 0.01 ~ 0.02m/s through each module flow velocity upwards, the coalescent module pressure drop of coarse of described liquefaction qi exhaustion amine unit within 0.005MPa, the pressure drop of nona modified fiber module is 0.005 ~ 0.01MPa, coalescent amine liquid size droplet diameter of growing up is 30 ~ 50 μm; Within after the process of described liquefaction qi exhaustion amine unit, the band amine liquid measure of liquefied gas is reduced to 20mg/L from 100 ~ 1000mg/L;
Described elementary quick separating unit removes the liquefied gas carried secretly in rich solution, the coalescent module pressure drop of coarse of described elementary quick separating unit within 0.005MPa, the pressure drop of nona modified fiber pre-separation module is 0.005 ~ 0.01MPa, coalescent oil droplet size of growing up is 30 ~ 50 μm; The flow velocity flowing through the rich solution of each module is 0.015 ~ 0.025m/s; Remove rear described liquefied gas entrainment to be reduced to fast within 100mg/L from 1000 ~ 5000mg/L;
The flow control of rich solution in described degree of depth separation equipment is 0.015 ~ 0.025m/s, and liquefied gas entrainment is reduced within 15mg/L fast from 50 ~ 100mg/L.
The isolated liquefied gas of the degree of depth is discharged by degree of depth separation equipment top oil bag and is removed follow up device in the lump with desulfurizing tower top liquefied gas, and after being separated, amine liquid removes subsequent production device again through flash tank.
8. method according to claim 7, is characterized in that, the pressure of described desulfurizing tower is 0.6 ~ 5.0Mpa, and temperature is 30 ~ 70 DEG C.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109355121A (en) * | 2018-12-19 | 2019-02-19 | 南京泰斯普化工工程技术有限公司 | A kind of high-efficiency desulfurization system of liquefied gas and device in Gas |
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| CN103031171A (en) * | 2012-12-26 | 2013-04-10 | 上海华畅环保设备发展有限公司 | Solvent foaming control method and device in amine desulfuration process of natural gas |
| CN103861423A (en) * | 2012-12-12 | 2014-06-18 | 中国石油化工股份有限公司 | Renewable absorption liquid for removing RSH and COS in acidic fluid |
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2015
- 2015-10-22 CN CN201510689870.9A patent/CN105195018B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861423A (en) * | 2012-12-12 | 2014-06-18 | 中国石油化工股份有限公司 | Renewable absorption liquid for removing RSH and COS in acidic fluid |
| CN103031171A (en) * | 2012-12-26 | 2013-04-10 | 上海华畅环保设备发展有限公司 | Solvent foaming control method and device in amine desulfuration process of natural gas |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109355121A (en) * | 2018-12-19 | 2019-02-19 | 南京泰斯普化工工程技术有限公司 | A kind of high-efficiency desulfurization system of liquefied gas and device in Gas |
| CN109355121B (en) * | 2018-12-19 | 2024-05-14 | 南京泰斯普化工工程技术有限公司 | Efficient desulfurization system for liquefied gas and gas |
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