Condensate oil desulfurization and rectification device

Abstract

The utility model discloses a gas condensate desulfurization and rectification device which comprises a fiber liquid film contactor, a rectification tower, a first cooler and a heater, the fiber liquid film contactor comprises a liquid film contactor shell used for containing the condensate oil for oxidative desulfurization reaction under the alkaline condition and a separation tank used for three-phase separation of a gas phase, a condensate oil phase and an alkaline solution phase, and the liquid film contactor shell is communicated with the separation tank; the rectifying tower is communicated with a condensate oil phase outlet of the separating tank, a light component branch pipeline is arranged at the top of the rectifying tower, and a heavy component branch pipeline is arranged at the bottom of the rectifying tower; the feeding end and the discharging end of the first cooler are communicated with the upper part of the rectifying tower; the heater is used for heating condensate oil at the lower part of the inner cavity of the rectifying tower. According to the utility model, the temperatures of the upper part and the lower part of the rectifying tower are different, the condensate oil is cut into light components and heavy components, and the generated disulfide and the original high-boiling-point sulfide in the condensate oil enter the heavy components due to high boiling point, so that the aims of desulfurizing the light components and deodorizing the heavy components of the condensate oil can be fulfilled.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the field of condensate oil processing technology, especially relates to a condensate oil desulfurization and rectification device. BACKGROUND

[0002] Condensate oil is the liquid phase component condensed from natural gas in condensate gas field, also called natural gasoline, and its main component is the mixture of C5~C8 hydrocarbon, and contains a small amount of C8 and above hydrocarbon. Condensate oil fraction is mostly between 20 DEG C and 200 DEG C, and has strong volatility, and therefore has a bad smell because of the inclusion of hydrogen sulfide, mercaptan, thiophene, sulfide and polysulfide.

[0003] The total sulfur content of condensate oil is mostly in thousands of mu g / g, and the content of H2S is generally low, generally within dozens of mu g / g, and the content of mercaptan accounts for about 70%. Because mercaptan has strong volatility, corrosiveness and bad smell, especially C1~C4 mercaptan, accounts for about 50% of the total mercaptan content, has relatively small molecular weight, and has a boiling point in the range of 6 DEG C~98 DEG C, and has stronger volatility, and is easy to volatilize during the loading, unloading and transportation of condensate oil, which seriously pollutes the environment, and has strong corrosiveness to carbon steel equipment and pipeline, and is easy to cause leakage accidents. Therefore, it is urgent to reduce the bad smell of condensate oil. CONTENT

[0004] The utility model aims at providing a condensate oil desulfurization and rectification device to solve the problems in the prior art.

[0005] To achieve the above object, the utility model provides a condensate oil desulfurization and rectification device, which comprises a fiber liquid membrane contactor, a rectification tower, a first cooler and a heater;The fiber liquid membrane contactor comprises a liquid membrane contactor shell for accommodating condensate oil alkaline condition oxidation desulfurization reaction and a separation tank for three-phase separation of gas phase, condensate oil phase and alkali solution phase, and the discharge port of the liquid membrane contactor shell and the feed port of the separation tank are in communication;The condensate oil phase outlet of the separation tank and the rectification tower are in communication, the top of the rectification tower is provided with a light component pipeline, and the bottom of the rectification tower is provided with a heavy component pipeline;The feed end and the discharge end of the first cooler are in communication with the upper part of the rectification tower;The heater is connected with the lower part of the rectification tower, and the heater is used for heating the condensate oil in the lower part of the cavity of the rectification tower.

[0006] Optionally, the condensate desulfurization and rectification device further comprises a reflux tank and a first circulating pump, the first cooler is arranged on a communication pipeline between the light component pipeline and the reflux tank, a gas phase outlet pipeline is connected to the top of the reflux tank, and the first circulating pump is arranged on a communication pipeline between the upper part of the rectification tower and the bottom of the reflux tank, and an outlet end of the first circulating pump is further connected to a light component outlet pipeline.

[0007] Optionally, the heavy component pipeline comprises a first heavy component pipeline and a second heavy component pipeline, the inlet ends of the first heavy component pipeline and the second heavy component pipeline are communicated with the lower part of the rectification tower, the heater is arranged on the first heavy component pipeline, and the outlet end of the first heavy component pipeline is communicated with the lower part of the rectification tower, and the second heavy component pipeline is provided with a second cooler, and the outlet end of the second cooler is connected to a heavy component outlet pipeline.

[0008] Optionally, the heater is a reboiler, the reboiler is internally provided with a working pipeline and a heating pipeline for heat exchange, the two ends of the working pipeline are respectively communicated with the first heavy component pipeline and the lower part of the rectification tower, the inlet end of the heating pipeline is communicated with a steam pipeline, and the outlet end of the heating pipeline is communicated with a condensed water pipeline.

[0009] Optionally, the feed end of the fiber liquid membrane contactor is communicated with a condensate pipeline, an air pipeline and a catalyst alkali solution pipeline, the alkali solution phase outlet of the separation tank is communicated with a waste alkali solution pipeline, and the gas phase outlet of the separation tank is communicated with a tail gas pipeline.

[0010] Optionally, the condensate desulfurization and rectification device further comprises a second circulating pump, the alkali solution phase outlet of the separation tank is communicated with an alkali solution reflux pipeline, the feed end of the second circulating pump is communicated with the catalyst alkali solution pipeline and the alkali solution reflux pipeline respectively, and the outlet end of the second circulating pump is communicated with the waste alkali solution pipeline and the upper part of the fiber liquid membrane contactor respectively.

[0011] Optionally, the separation tank is internally provided, in sequence according to the fluid flow direction, with a separation cavity, a phase separation assembly and a phase separation cavity, the separation tank is arranged below the liquid membrane contactor shell, and the liquid membrane contactor shell is communicated with the separation cavity, the phase separation assembly comprises, in sequence according to the fluid flow direction, a distribution hole plate, a flow guide plate and a mixed wire mesh coalescing element, the top of the phase separation cavity is provided with a gas separation bag, the gas separation bag is communicated with the tail gas pipeline, and the condensate phase outlet and the alkali solution phase outlet are arranged at the upper and lower ends of the phase separation cavity respectively.

[0012] Optionally, the distribution hole plate comprises a first plate body which is detachably connected to the liquid membrane contactor shell, a plurality of through holes are formed in the first plate body, and the through holes are distributed axially along the fluid flow direction.

[0013] Optionally, the flow guide plate comprises a first shell detachably connected with the liquid membrane contactor shell, and a plurality of groups of corrugated plates arranged in parallel are arranged inside the first shell and arranged along the fluid flow direction.

[0014] Optionally, the liquid membrane contactor shell is internally provided with liquid membrane filaments for contacting the material fluid and the reaction liquid, the liquid membrane contactor shell is detachably connected with a filament suspension beam inside the liquid membrane contactor shell, the filament suspension beam is perpendicular to the central axis of the liquid membrane contactor shell, one end of the liquid membrane filament is detachably connected with the filament suspension beam, and the liquid membrane filament is arranged in a drooping manner under the action of its own gravity.

[0015] Compared with the prior art, the utility model has the advantages and technical effects that:

[0016] The liquid membrane contactor shell contains the catalytic oxidation reaction of condensate oil under alkaline conditions, converts low-boiling-point small-molecule mercaptans in the condensate oil into high-boiling-point disulfides, and solves the problem of odor of the condensate oil; the three phases of gas phase, condensate oil phase and alkali solution phase in the product obtained after the reaction and unreacted substances are separated through the separation tank, the condensate oil phase obtained through the separation is introduced into the rectifying column, the condensate oil is light at the top and heavy at the bottom due to different densities based on different alkyls in the condensate oil components, the condensate oil located at the top of the rectifying column is cooled through the first cooler, the condensate oil located at the bottom of the rectifying column is heated through the heater, the temperatures of the two positions of the upper part and the lower part of the rectifying column are different, and due to different boiling points of light components and heavy components in the condensate oil, the light components located at the bottom of the rectifying column move upward after boiling, the heavy components located at the top of the rectifying column move downward after cooling, the condensate oil is further cut into light components and heavy components, and the cut light components and heavy components are discharged in time through the light component pipeline and the heavy component pipeline, and the generated disulfides enter the heavy components due to high boiling points and high-boiling-point sulfides originally in the condensate oil, so that the purposes of desulfurization of the light components of the condensate oil and deodorization of the heavy components are achieved. BRIEF DESCRIPTION OF DRAWINGS

[0017] In order to more clearly illustrate the technical scheme in the embodiments of the utility model or the prior art, the drawings needed to be used in the embodiments will be briefly introduced below, and obviously, the drawings in the following description are only some embodiments of the utility model, and other drawings can be obtained by those skilled in the art without creating labor under the premise of the drawings.

[0018] Figure 1 It is a structure schematic view of the condensate oil desulfurization and rectification device of the utility model;

[0019] Figure 2 It is a structure schematic view of the distributor of the utility model;

[0020] Figure 3 It is liquid membrane fiber distribution schematic view of the utility model;

[0021] Figure 4 It is distribution orifice plate structure schematic view of the utility model;

[0022] Figure 5 It is mixed silk screen coalescing element structure schematic view of the utility model;

[0023] Wherein, 1, filter, 2, liquid membrane contactor shell, 3, distributor, 4, liquid membrane fiber, 5, separation tank, 6, gas distribution package, 7, distribution orifice plate, 8, guide plate, 9, mixed silk screen coalescing element, 10, second circulating pump, 11, rectifying tower, 13, first cooler, 14, reflux tank, 15, first circulating pump, 16, heater, 17, second cooler, 18, second heavy component pipeline, 21, condensate pipeline, 22, air pipeline, 23, catalyst lye pipeline, 24, lye reflux pipeline, 25, tail gas pipeline, 26, waste lye pipeline, 27, desulfurized condensate pipeline, 28, light component pipeline, 29, first light component pipeline, 30, light component discharge pipeline, 31, second light component pipeline, 32, gas phase discharge pipeline, 33, second heavy component pipeline, 34, heavy component discharge pipeline, 35, steam pipeline, 36, condensate pipeline. DETAILED DESCRIPTION

[0024] It should be noted that the embodiments in the utility model and the features in the embodiments can be combined with each other without conflict. The described embodiments are only part of the embodiments of the utility model, not all the embodiments. All other embodiments obtained by the ordinary skill in the art without creative labor belong to the scope of protection of the utility model. The utility model will be described in detail below with reference to the drawings and in combination with the embodiments.

[0025] Referring to Figures 1-5 The utility model provides a kind of condensate oil desulfurization and rectifying device, including fiber liquid membrane contactor, rectifying tower 11, first cooler 13 and heater 16;Fiber liquid membrane contactor includes liquid membrane contactor shell 2 for accommodating condensate oil alkaline condition oxidation desulfurization reaction and separation tank 5 for the separation of three phases of gas phase, condensate oil phase and alkali solution phase, the discharge port of liquid membrane contactor shell 2 and the feed port of separation tank 5 are communicated;Rectifying tower 11 is communicated with the condensate oil phase outlet of separation tank 5, and the top of rectifying tower 11 is provided with light component pipeline 28, and the bottom of rectifying tower 11 is provided with heavy component pipeline;The feed end and discharge end of first cooler 13 are all communicated with the upper portion of rectifying tower 11;Heater 16 is connected with the lower portion of rectifying tower 11, and heater 16 is used to heat the condensate oil in the lower portion of the cavity of rectifying tower 11.

[0026] In the present embodiment, the condensate alkaline condition oxidation desulfurization reaction refers to the oxidation reaction of C1-C4 mercaptan in the condensate with oxygen in the air in the presence of a catalyst and lye, and the reaction is as follows:

[0027] 2RSH+1 / 2O2→RSSR+H2O

[0028] The reaction actually goes through the following two processes:

[0029] RSH+NaOH→NaSR+H2O

[0030] 2NaSR+1 / 2O2+H2O→2NaOH+RSSR

[0031] In the above reaction, R refers to C1-C4 alkyl. In the present reaction process, the smaller the molecular weight of the mercaptan, the faster the reaction rate and the more complete the removal, while high molecular weight mercaptan and other sulfides are difficult to react under the present conditions. The present technology converts low-boiling small molecular mercaptan in the condensate into high-boiling disulfide by catalytic oxidation.

[0032] The utility model discloses a liquid membrane contactor shell 2 contains condensate under alkaline condition catalytic oxidation reaction, converts low-boiling small molecular mercaptan in the condensate into high-boiling disulfide, solves the stench problem of condensate, separates the gas phase, condensate phase and alkali solution phase of the product obtained after reaction and unreacted substances through separation tank 5, and the separated condensate phase enters rectifying column 11, based on the different alkyl of condensate components, condensate appears light on top and heavy on bottom due to the different densities, and the utility model is cooled to the condensate above rectifying column 11 through first cooler 13, and the condensate below rectifying column 11 is heated through heater 16, so that the temperatures of the upper and lower parts of rectifying column 11 are different, and due to the different boiling points of light components and heavy components in condensate, the light component below rectifying column boils and moves upward, and the heavy component above rectifying column cools down and moves downward, further cutting condensate into light components and heavy components, and discharging the cut light components and heavy components in time through light component pipeline and heavy component pipeline, and the generated disulfide enters heavy components with the original high-boiling sulfides in condensate due to high boiling point, so that the purposes of condensate light component desulfurization and heavy component deodorization are realized.

[0033] The utility model adopts rectifying cutting method to obtain low-sulfur condensate light component and condensate heavy component with obviously reduced stench smell, the low-sulfur condensate light component can be used as oil blending, the condensate heavy component with obviously reduced stench smell and corrosion can be used as deep processing raw material, the condensate light component has high economic benefit, the deep processability of condensate heavy component is improved, and the overall benefit of condensate is obviously improved.

[0034] In the embodiment, the first cooler 13 is independent, that is, the feed pipe and the discharge pipe of the first cooler 13 are communicated with the upper part of the rectifying tower 11, the condensate oil in the upper part of the rectifying tower 11 is directly cooled by the first cooler 13, and a circulating pump is arranged at any position of the discharge pipe and the feed pipe as a power source. The light component pipe 28 is used as a light component discharge pipe, and a pump is additionally arranged on the light component pipe 28 as a power source to extract the separated light component from the rectifying tower 11.

[0035] In the embodiment, the first cooler 13 and the light component pipe 28 are combined to realize the functions of cooling and discharging. Preferably, the condensate oil desulfurization and rectification device further comprises a reflux tank 14 and a first circulating pump 15, the first cooler 13 is arranged on a communication pipe between the light component pipe 28 and the reflux tank 14, the top of the reflux tank 14 is connected and communicated with a gas phase discharge pipe 32, the first circulating pump 15 is arranged on a communication pipe between the upper part of the rectifying tower 11 and the bottom of the reflux tank 14, and the outlet end of the first circulating pump 15 is further connected and communicated with a light component discharge pipe 30. In the embodiment, the pipe between the first cooler 13 and the reflux tank 14 is a first light component pipe 29, and the pipe between the first circulating pump 15 and the upper part of the rectifying tower 11 is a second light component pipe 31. In operation, the first circulating pump 15 extracts the condensate oil above the rectifying tower 11 as a power source, the condensate oil enters the first cooler 13 through the light component pipe 28 for cooling, the cooled condensate oil enters the reflux tank 14 through the first light component pipe 29, a part of the condensate oil in the reflux tank 14 still exists in a gas phase, the condensate oil in the gas phase is discharged from the reflux tank 14 through the gas phase discharge pipe 32, and the condensate oil in a liquid phase is returned to the rectifying tower 11 through the first circulating pump 15 and the second light component pipe 31 to cool the condensate oil in the upper part of the rectifying tower 11. When the separated light component needs to be discharged, the first circulating pump 15 extracts the light component in the liquid phase at the bottom of the reflux tank 14 and discharges the light component from the reflux tank 14 through the light component discharge pipe 30.

[0036] In the embodiment, the heater 16 can adopt various ways, such as, built-in heating method of arranging heating wires or other heating mechanisms in the lower part of the inner cavity of the rectifying tower 11; heating method of arranging heating wires or other heating mechanisms on the lower tower wall of the rectifying tower 11; external heating method of heating the condensate oil in the lower part of the rectifying tower 11 after leading out; and the like. Preferably, the heavy component pipeline comprises a first heavy component pipeline 33 and a second heavy component pipeline 18, the inlet ends of the first heavy component pipeline 33 and the second heavy component pipeline 18 are communicated with the lower part of the rectifying tower 11; the heater 16 is arranged on the first heavy component pipeline 33, and the outlet end of the first heavy component pipeline 33 is communicated with the lower part of the rectifying tower 11; the second cooling device 17 is arranged on the second heavy component pipeline 18, and the outlet end of the second cooling device 17 is connected with and communicated with the heavy component discharge pipeline 34. The embodiment adopts the external heating method to heat the condensate oil in the lower part of the rectifying tower 11, which is convenient for detecting the temperature of the condensate oil in the lower part of the rectifying tower 11. When the separated heavy component needs to be discharged from the rectifying tower 11, under the action of the internal pressure of the rectifying tower 11, the heavy component enters the second cooling device 17 through the second heavy component pipeline 18 to be cooled, and the cooled heavy component is discharged through the heavy component discharge pipeline 34. The embodiment further heats the condensate oil in the first heavy component pipeline 33 through the heater 16, and the heated condensate oil flows back to the lower part of the rectifying tower 11.

[0037] Further optimization scheme, the heater 16 is a reboiler, the reboiler is internally provided with a working pipeline and a heating pipeline for heat exchange, the two ends of the working pipeline are respectively communicated with the first heavy component pipeline 33 and the lower part of the rectifying tower 11, the inlet end of the heating pipeline is communicated with a steam pipeline 35, and the outlet end of the heating pipeline is communicated with a condensed water pipeline 36. The embodiment heats the condensate oil in the form of heat exchange, the condensate oil in the working pipeline is heated by the steam in the steam pipeline 35, the heated condensate oil flows back to the lower part of the rectifying tower 11, the cooled steam and condensed water are discharged through the condensed water pipeline 36, and compared with other heating forms, since the heating temperature of the condensate oil in the embodiment is within 200℃, about 150℃, the required heating amount is small, and waste heat in other production processes can be fully utilized for heating.

[0038] In the working process of the utility model, the temperature of the condensate oil above and below the rectifying tower 11 needs to be detected and controlled, the cooling process and the heating process of the embodiment are both carried out by the external leading mode, and the temperature detection is carried out by the temperature detector in the leading pipeline. The pressure at the top of the rectifying tower 11 is controlled in the range of 0.05MPa (G) ~ 0.15MPa (G), part of the condensate oil at the bottom of the rectifying tower 11 is heated by the heater 16 and then returns to the rectifying tower 11, and the bottom temperature is controlled in the range of 130 DEG C ~ 160 DEG C; part of the condensate oil at the top of the rectifying tower 11 is cooled by the first cooler 13 and then returns to the rectifying tower 11, the reflux ratio at the top of the tower is 0.3 ~ 1.0, the reflux temperature is 45 DEG C ~ 55 DEG C, and the temperature at the upper part of the rectifying tower 11 is controlled in the range of 90 DEG C ~ 100 DEG C. The condensate oil light component with the rectification cutting temperature below 100 DEG C, the mercaptan content less than 20 μg / g and the total sulfur content less than 50 μg / g is obtained by the reflux at the top of the tower, and the condensate oil heavy component with the rectification cutting temperature above 100 DEG C and the odor greatly reduced is obtained after the cooling at the bottom of the tower.

[0039] Preferably, the feed end of the fiber liquid membrane contactor is communicated with a condensate oil pipeline 21, an air pipeline 22 and a catalyst lye pipeline 23, the alkali solution phase outlet of the separation tank 5 is communicated with a waste lye pipeline 26, and the gas phase outlet of the separation tank 5 is communicated with a tail gas pipeline 25. In the working process of the embodiment, the condensate oil raw material is added into the fiber liquid membrane contactor through the condensate oil pipeline 21, the air is added into the fiber liquid membrane contactor through the air pipeline 22, and the catalyst and the alkali solution are added into the fiber liquid membrane contactor through the catalyst lye pipeline 23. In the embodiment, the air pipeline 22 can also adopt an oxygen pipeline, but since the reaction disclosed in the utility model needs a small amount of oxygen, the oxygen content in the air can meet the oxygen demand of the reaction. The catalyst and the alkali solution after the reaction are discharged from the separation tank 5 through the waste lye pipeline 26, and the excess gas in the separation tank 5 is discharged through the tail gas pipeline 25. In the embodiment, the catalyst alkali solution is the aqueous solution of sodium hydroxide or potassium hydroxide with 100 μg / g-200 μg / g sulfonated titanium phthalocyanine cobalt or poly titanium phthalocyanine catalyst dissolved, the volume ratio of the air to the condensate oil is 0.5 ~ 1.0, and the volume ratio of the lye to the condensate oil is 0.3 ~ 0.6.

[0040] Further optimization scheme, a condensate desulfurization and rectification device further comprises a second circulating pump 10, the alkali solution phase outlet of the separation tank 5 is communicated with an alkali solution reflux pipeline 24, the feed end of the second circulating pump 10 is communicated with the catalyst alkali solution pipeline 23 and the alkali solution reflux pipeline 24 respectively, and the outlet end of the second circulating pump 10 is communicated with the waste alkali solution pipeline 26 and the upper part of the fiber liquid membrane contactor respectively. When the embodiment works, since the catalyst and the alkali solution in the reaction only play a catalytic role and an alkaline ring, the alkaline concentration and the catalyst remain basically unchanged, so the embodiment re-injects the excess catalyst and the alkali solution in the separation tank 5 into the upper part of the liquid membrane contactor shell 2 through the second circulating pump 10 and the alkali solution reflux pipeline 24, participates in the condensate alkaline condition oxidation desulfurization reaction again, and the catalyst and the alkali solution are recycled. When the catalyst and the alkali solution are reduced in solubility, or the demand for the catalyst and the alkali solution in the reaction increases, new catalyst alkali solution is injected into the liquid membrane contactor shell 2 through the catalyst alkali solution pipeline 23 and the second circulating pump 10, and the new and old catalyst alkali solutions participate in the condensate alkaline condition oxidation desulfurization reaction together. When it is necessary to replace the old catalyst alkali solution, the old catalyst alkali solution can be discharged from the separation tank 5 through the waste alkali solution pipeline 26 and the second circulating pump 10, and then new catalyst alkali solution is injected into the liquid membrane contactor shell 2 through the catalyst alkali solution pipeline 23 and the second circulating pump 10.

[0041] Preferably, the separation tank 5 is sequentially provided with a separation cavity, a phase separation assembly and a phase separation cavity inside in the fluid flow direction, the separation tank 5 is arranged below the liquid membrane contactor shell 2, and the liquid membrane contactor shell 2 is communicated with the separation cavity; the phase separation assembly comprises a distribution hole plate 7, a flow guide plate 8 and a mixed wire mesh coalescing element 9 arranged in sequence in the fluid flow direction; the phase separation cavity is provided with a gas pack 6 at the top, the gas pack 6 is communicated with a tail gas pipeline 25, and the condensate phase outlet and the alkali solution phase outlet are arranged at the upper and lower ends of the phase separation cavity respectively. The pipeline between the condensate phase outlet and the separation tank 5 is a desulfurized condensate pipeline 27.

[0042] In the embodiment, the product and unreacted substance after the condensate is oxidized and desulfurized under alkaline conditions, which are collectively referred to as the post-reaction substance, enters the separation cavity of the separation tank 5 through the liquid membrane contactor shell 2, and the post-reaction substance enters the phase separation cavity through the distribution hole plate 7, the flow guide plate 8 and the mixed wire mesh coalescing element 9 in turn. The flow rate of the post-reaction substance is reduced through the distribution hole plate 7, so that the gas phase, the condensate phase and the alkaline solution phase in the post-reaction substance are preliminarily separated. The preliminary separation is based on the principle that the three phases are immiscible. The flow rate of the post-reaction substance is further limited through the flow guide plate 8, and the gas phase, the condensate phase and the alkaline solution phase preliminarily separated are layered and guided to transmit. The three phases are uniformly distributed through the distribution hole plate 7 and the flow guide plate 8 and slowly pass through the mixed wire mesh coalescing element 9. Under the action of the mixed wire mesh coalescing element 9, the alkaline solution phase in the condensate phase is coalesced and separated, the condensate phase in the alkaline solution phase is coalesced and separated, and the separation speed of the condensate phase and the alkaline solution is accelerated. After the above-mentioned effects, the gas phase, the condensate phase and the alkaline solution phase in the post-reaction substance are layered and arranged in the phase separation cavity.

[0043] In the embodiment, the mixed wire mesh coalescing element 9 includes hydrophilic wire mesh and oleophilic wire mesh mixed together. The post-reaction substance is further coalesced and separated under the surface tension of the hydrophilic wire mesh and the oleophilic wire mesh. The free alkaline solution entrained in the oil phase is not more than 10 μg / g, and the free oil phase entrained in the alkaline solution is not more than 30 μg / g, so as to accelerate the separation speed of the oil phase and the alkaline solution, and reduce the volume of the separation tank by 30% to 50%. The gas-liquid level of the tail gas and the condensate is controlled to be about 50%, the tail gas is sent to the oil and gas recovery facility and the tail gas treatment facility, and the condensate-alkaline solution interface level is controlled to be about 50%.

[0044] Preferably, the distribution hole plate 7 includes a first plate body detachably connected with the liquid membrane contactor shell 2. A plurality of through holes are formed in the first plate body and are distributed along the fluid flow direction. In the embodiment, the post-reaction substance flows through the through holes in the distribution hole plate 7. The flow rate of the post-reaction substance is reduced through the interception of the non-through area of the first plate body, so that the gas phase, the condensate phase and the alkaline solution phase in the post-reaction substance are preliminarily separated. Of course, the flow rate of the post-reaction substance can be further controlled by controlling the number and area of the through holes.

[0045] Preferably, the flow guide plate 8 includes a first shell detachably connected with the liquid membrane contactor shell 2. A plurality of groups of corrugated plates are arranged in parallel inside the first shell and are arranged along the fluid flow direction. The three phases of the gas phase, the condensate phase and the alkaline solution phase are layered after the preliminary separation. The three phases after the layering pass through the gaps between the adjacent corrugated plates, so as to further limit the flow rate of the post-reaction substance, improve the separation time of the three phases, and guide and transmit the gas phase, the condensate phase and the alkaline solution phase preliminarily separated.

[0046] Preferably, the liquid membrane contactor shell 2 is internally provided with liquid membrane fiber filaments 4 for contacting the material fluid and the reaction liquid, the liquid membrane contactor shell 2 is detachably connected with a fiber filament suspension beam which is perpendicular to the central axis of the liquid membrane contactor shell 2, one end of the liquid membrane fiber filament 4 is detachably connected with the fiber filament suspension beam, and the liquid membrane fiber filament is arranged in a drooping manner under the action of its own gravity. The liquid membrane contactor shell 2 is further provided with a distributor 3, which is arranged on the side of the fiber filament suspension beam away from the liquid membrane fiber filament; the condensate oil pipeline 21, the air pipeline 22 and the catalyst lye pipeline 23 are jointly communicated on the same filter 1, and the outlet end of the filter 1 and the inlet end of the distributor 3 are in communication. The liquid membrane fiber filament 4 is a hydrophilic modified slender fiber filament, the surface of which is treated by a special hydrophilic modification technology, the hydrophilic angle is 1-3°, and the single fiber filament is in a continuous corrugated or spiral shape.

[0047] The sulfur-containing foul-smelling condensate oil has a pressure requirement in the range of 0.2MPa(G)-1.0MPa(G) and a temperature requirement in the range of 10℃-50℃, the condensate oil, the catalyst alkali solution and the air are combined into one, filtered through the filter 1 with a filtering precision in the range of 50μg / g-150μg / g, and then enter the liquid membrane contactor shell 2 after removing mechanical impurities, the air, the condensate oil and the catalyst alkali solution are evenly distributed between the liquid membrane fiber filaments through the distributor 3, the three phases are in full contact between the liquid membrane fiber filaments, and under the action of the catalyst, more than 80% of the low-boiling-point C1-C4 mercaptans in the condensate oil are converted into high-boiling-point disulfides by reacting with oxygen in the air, and the reacted substances enter the separation chamber under the action of gravity.

[0048] Scheme 1:

[0049] A certain oil and gas field provides a sulfur-containing foul-smelling condensate oil sample, the hydrogen sulfide content is 17μg / g, the total mercaptan content is 2740μg / g, the C1-C4 mercaptan content is 1576μg / g, and the total sulfur content is 3653μg / g, the condensate oil desulfurization and rectification device is used, the desulfurization liquid membrane contactor operating pressure is 0.2MPa(G), the gas-hydrocarbon volume ratio is 0.5, the alkali-hydrocarbon volume ratio is 0.3, the gas-liquid separation level control is 45%, the separation tank level control is 45%, the rectification tower top operating pressure is 0.05MPa(G), the tower bottom temperature is in the range of 130-140℃, the tower top reflux ratio is 0.3, the reflux temperature is 45℃, and the tower top temperature is in the range of 90-95℃. The obtained condensate oil light component has a mercaptan content of 18μg / g and a total sulfur content of 47μg / g, and the condensate oil heavy component has a significantly reduced foul-smelling odor compared with the raw material.

[0050] Scheme 2:

[0051] A certain oil and gas field provides a sulfur-containing foul-smelling condensate oil sample, the hydrogen sulfide content is 17 μg / g, the total content of mercaptan is 2740 μg / g, wherein the content of C1-C4 mercaptan is 1576 μg / g, the total sulfur content is 3653 μg / g, the condensate oil desulfurization and rectification device is adopted, the operating pressure of desulfurization liquid membrane contactor is 0.5 MPa (G), the volume ratio of gas hydrocarbon is 0.7, the volume ratio of alkali hydrocarbon is 0.6, the liquid level control of gas separation package is 45%, the boundary level control of separation tank is 45%, the operating pressure at the top of rectification tower is 0.09 MPa (G), the bottom temperature is in the range of 140-150 DEG C, the reflux ratio at the top of tower is 0.7, the reflux temperature is 45 DEG C, and the top temperature is in the range of 90-95 DEG C. The obtained condensate oil light component mercaptan content is 16 μg / g, the total sulfur content is 35 μg / g, and the foul-smelling odor of condensate oil heavy component is obviously reduced compared with the raw material.

[0052] Scheme 3:

[0053] A certain oil and gas field provides a sulfur-containing foul-smelling condensate oil sample, the hydrogen sulfide content is 17 μg / g, the total content of mercaptan is 2740 μg / g, wherein the content of C1-C4 mercaptan is 1576 μg / g, the total sulfur content is 3653 μg / g, the condensate oil desulfurization and rectification device is adopted, the operating pressure of desulfurization liquid membrane contactor is 0.5 MPa (G), the volume ratio of gas hydrocarbon is 0.7, the volume ratio of alkali hydrocarbon is 0.6, the liquid level control of gas separation package is 45%, the boundary level control of separation tank is 45%, the operating pressure at the top of rectification tower is 0.09 MPa (G), the bottom temperature is in the range of 140-150 DEG C, the reflux ratio at the top of tower is 0.7, the reflux temperature is 45 DEG C, and the top temperature is in the range of 90-95 DEG C. The obtained condensate oil light component mercaptan content is 16 μg / g, the total sulfur content is 35 μg / g, and the foul-smelling odor of condensate oil heavy component is obviously reduced compared with the raw material.

[0054] The above examples are only used to help understand the method and its core idea of the application; meanwhile, for those skilled in the art, according to the idea of the application, the specific implementation and application range can be changed, and the content of the specification should not be understood as the limitation of the application.

[0055] It should be understood that the term "and / or" used herein only describes the association relationship of the associated objects, which means that there can be three relationships, for example, A and / or B, which can represent the three cases of A alone, A and B together, and B alone. In addition, the character " / " herein generally represents an "or" relationship between the front and rear associated objects.

[0056] In the description of the utility model, need understanding is, the term "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and so on indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawing, just for the convenience of describing the utility model, and it is not indicated or implied that the indicated device or element must have a particular orientation, a particular orientation and operation, so it can not be understood as a limitation on the utility model.

[0057] The above-described embodiments are merely preferred modes of the utility model, and do not limit the scope of the utility model, and various modifications and improvements to the technical solutions of the utility model made by those skilled in the art without departing from the design spirit of the utility model shall fall within the protection scope of the utility model claimed.

Claims

1. A condensate desulfurization and rectification apparatus, characterized by comprising: The application relates to a fiber liquid membrane contactor, which comprises a liquid membrane contactor shell (2) for containing a condensate alkaline condition oxidative desulfurization reaction and a separation tank (5) for separating a gas phase, a condensate phase and an alkaline solution phase, a discharge port of the liquid membrane contactor shell (2) and a feed port of the separation tank (5) are communicated. A rectifying tower (11) is communicated with a condensate phase outlet of the separation tank (5), a top of the rectifying tower (11) is provided with a light component pipeline (28), and a bottom of the rectifying tower (11) is provided with a heavy component pipeline. A first cooler (13) is communicated with an upper portion of the rectifying tower (11). A heater (16) is connected with a lower portion of the rectifying tower (11), and the heater (16) is used for heating condensate in a lower portion of a cavity of the rectifying tower (11). A reflux tank (14) and a first circulating pump (15) are further included, the first cooler (13) is communicated with a communication pipeline between the light component pipeline (28) and the reflux tank (14), a top of the reflux tank (14) is connected and communicated with a gas phase discharge pipeline (32), the first circulating pump (15) is communicated with a communication pipeline between an upper portion of the rectifying tower (11) and a bottom of the reflux tank (14), and an outlet end of the first circulating pump (15) is further connected and communicated with a light component discharge pipeline (30).

2. The condensate desulphurization and rectification unit as claimed in claim 1, wherein, The heavy component pipeline comprises a first heavy component pipeline (33) and a second heavy component pipeline (18), inlet ends of the first heavy component pipeline (33) and the second heavy component pipeline (18) are communicated with a lower portion of the rectifying tower (11), the heater (16) is arranged on the first heavy component pipeline (33), and an outlet end of the first heavy component pipeline (33) is communicated with the lower portion of the rectifying tower (11), and the second heavy component pipeline (18) is provided with a second cooler (17), and an outlet end of the second cooler (17) is connected and communicated with a heavy component discharge pipeline (34).

3. The condensate desulphurization and rectification unit as claimed in claim 1, wherein, The heater (16) is a reboiler, the reboiler is internally provided with a working pipeline and a heating pipeline for heat exchange, two ends of the working pipeline are respectively communicated with the first heavy component pipeline (33) and the lower portion of the rectifying tower (11), an inlet end of the heating pipeline is communicated with a steam pipeline (35), and an outlet end of the heating pipeline is communicated with a condensed water pipeline (36).

4. The condensate desulfurization and rectification apparatus according to claim 3, wherein A condensate pipeline (21), an air pipeline (22) and a catalyst alkaline solution pipeline (23) are communicated with an inlet end of the fiber liquid membrane contactor, a waste alkaline solution pipeline (26) is communicated with an alkaline solution phase outlet of the separation tank (5), and a tail gas pipeline (25) is communicated with a gas phase outlet of the separation tank (5).

5. The condensate desulfurization and rectification apparatus according to claim 1, wherein ​ 6. The condensate desulfurization and rectification apparatus according to claim 5, wherein The second circulating pump (10) is communicated with the catalyst alkali solution pipeline (23) and the alkali solution reflux pipeline (24) respectively, and the outlet of the second circulating pump (10) is communicated with the waste alkali solution pipeline (26) and the upper part of the fiber liquid membrane contactor respectively.

7. The condensate desulphurization and rectification unit as claimed in claim 5, wherein, The separation tank (5) is sequentially provided with a separation cavity, a phase separation assembly and a phase separation cavity in the fluid flow direction, and the separation tank (5) is arranged below the liquid membrane contactor shell (2) and communicated with the separation cavity; the phase separation assembly comprises a distribution hole plate (7), a flow guide plate (8) and a mixed wire mesh coalescing element (9) arranged in the fluid flow direction; the top of the phase separation cavity is provided with a gas pack (6) communicated with the tail gas pipeline (25), and the condensate oil phase outlet and the alkali solution phase outlet are arranged at the upper and lower ends of the phase separation cavity.

8. The condensate desulfurization and rectification apparatus according to claim 7, wherein The distribution hole plate (7) comprises a first plate body detachably connected with the liquid membrane contactor shell (2), and a plurality of through holes are formed in the first plate body and distributed in the fluid flow direction.

9. The condensate desulfurization and rectification apparatus according to claim 7, wherein The flow guide plate (8) comprises a first shell body detachably connected with the liquid membrane contactor shell (2), and a plurality of groups of corrugated plates are arranged in parallel in the first shell body and arranged in the fluid flow direction.

10. The condensate desulphurization and rectification unit as claimed in claim 1, wherein, The liquid membrane contactor shell (2) is provided with liquid membrane fibers (4) for contacting the material fluid and the reaction liquid, and a fiber silk hanging beam is detachably connected in the liquid membrane contactor shell (2), the fiber silk hanging beam is perpendicular to the central axis of the liquid membrane contactor shell (2), one end of the liquid membrane fiber (4) is detachably connected with the fiber silk hanging beam, and the liquid membrane fiber (4) is arranged under the action of its own gravity.

Images