CN204455032U - The device of recovering of vaporized hydrocarbons and extraction regenerated methanol - Google Patents
The device of recovering of vaporized hydrocarbons and extraction regenerated methanol Download PDFInfo
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- CN204455032U CN204455032U CN201520071000.0U CN201520071000U CN204455032U CN 204455032 U CN204455032 U CN 204455032U CN 201520071000 U CN201520071000 U CN 201520071000U CN 204455032 U CN204455032 U CN 204455032U
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Abstract
The utility model discloses the device of a kind of recovering of vaporized hydrocarbons and extraction regenerated methanol.Comprise: condensation, First Heat Exchanger, prewashing tower, flasher, extractor, azeotrope separation device and methanol rectifying system.First Heat Exchanger exports with the cooled coal gas of condensation and is connected, and First Heat Exchanger has cold de-oiling gas entry and the first gas exit.Prewashing tower comprises the outlet of the second gas entry, cold methanol entrance and the first methanol solution, and the second gas entry is connected with the first gas exit, and de-oiling gas exit is connected with cold de-oiling gas entry.Flasher has the first methanol solution entrance and the outlet of the second methanol solution, and the first methanol solution entrance is connected by the second interchanger between exporting with the first methanol solution.Extractor comprises the second methanol solution entrance, the 3rd methanol solution outlet, and the second methanol solution entrance exports with the second methanol solution and is connected.Device of the present utility model, recovering of vaporized hydrocarbons rate is high, the lightweight oil quality that reclaims is high, lightweight oil and the mutual pollution level of methyl alcohol low.
Description
Technical field
The utility model relates to the field of purification of the coal gas that gasification is produced, and especially relates to the device of a kind of recovering of vaporized hydrocarbons and extraction regenerated methanol.
Background technology
For some Coal Gasification Technology, such as pressurization static bed Coal Gasification Technology, the pressurised fluidized bed Coal Gasification Technology of multistage etc., produce the byproduct that some have higher economic worth in coal gasification course simultaneously, must effectively be separated and reclaim, to improve the economy of gasification technology, avoid gas purification difficult treatment simultaneously or cause environmental pollution.
Some byproducts comprise tar products, the delivery medium etc. of middle oil production and clean or white or gasification use itself.General definition tar is the organic substance that density ratio water is large, and middle oil is the organic substance that density ratio water is little, and both boiling point is all high than water; Lightweight oil be organic substance and boiling point that density ratio water is little and water close to or lower straight-chain paraffin oil or aromatic ring hydrocarbon ils.
The current recovery method to these byproducts or delivery medium is that the high temperature oil-containing raw gas vapourizing furnace adopts washing Quench, reduces temperature and the oil product condensation of different boiling is separated again, reclaim oil in heavy tar and part with this; Raw gas reclaims remaining middle oil and part lightweight oil after being cooled to normal temperature.But still containing a large amount of lightweight oils and a small amount of mink cell focus in the coal gas of normal temperature, following impact is caused on follow-up system:
1, in coal gas, the existence of above-mentioned oils can cause equipment dirty stifled, reduces the performance of equipment, such as interchanger heat exchange property, washing absorption tower separation performance etc.
If a large amount of oils removes not thorough in 2 coal gas, methanol loop loop is washed to low-temperature rectisol master and pollutes, low temperature methanol cleaning voltinism energy can be reduced.
3, in order to thoroughly remove the oils in coal gas, normal temperature quantity of methyl alcohol or the low-temp methanol amount of conventional washing needs are larger, and cause the ability of the regenerating unit of methanol solution and consume large, methanol loop amount is large.
4, contain methyl alcohol in the lightweight oil that traditional method reclaims, cause lightweight oil Quality Down, or reuse difficulty.
5, the loss of methyl alcohol is also caused in lightweight oil containing methyl alcohol.
Utility model content
The utility model is intended to solve one of technical problem in correlation technique at least to a certain extent.
For this reason, the lightweight oil quality the utility model proposes the device of a kind of recovering of vaporized hydrocarbons and extraction regenerated methanol, recovering of vaporized hydrocarbons rate is high, reclaiming is high, lightweight oil and the mutual pollution level of methyl alcohol low.
According to the recovering of vaporized hydrocarbons of the utility model embodiment and the device of extraction regenerated methanol, comprise: carry out to coal gas the condensation of condensation of lowering the temperature, described condensation comprises for entering containing the first gas entry of oil gas, cooled coal gas outlet and the outlet of the first lightweight oil; First Heat Exchanger, described First Heat Exchanger and described cooled coal gas export and are connected for receiving the coal gas after being separated of discharging from described condensation, and described First Heat Exchanger has cold de-oiling gas entry and the first gas exit; Prewashing tower, described prewashing tower comprises the outlet of the second gas entry, cold methanol entrance, de-oiling gas exit and the first methanol solution, and described second gas entry is connected with described first gas exit, and described de-oiling gas exit is connected with described cold de-oiling gas entry; Flasher, described flasher has the outlet of the first methanol solution entrance, pneumatic outlet and the second methanol solution, described first methanol solution entrance is connected by the second interchanger between exporting with described first methanol solution, and described second interchanger heats the methanol solution of discharging from described first methanol solution outlet; Extractor, described extractor comprises the second methanol solution entrance, extraction water import, the second lightweight oil outlet and the outlet of the 3rd methanol solution, and described second methanol solution entrance exports with described second methanol solution and is connected; Azeotrope separation device, described azeotrope separation device comprises the 3rd methanol solution entrance, the 3rd lightweight oil outlet, the 4th methanol solution outlet and non-condensable gas outlet, described 3rd methanol solution entrance exports with described 3rd methanol solution and is connected, and described 3rd lightweight oil outlet is connected with described second methanol solution entrance; Methanol rectifying system, described methanol rectifying system comprises the 4th methanol solution entrance, pure methanol outlet and water out, and described 4th methanol solution entrance exports with described 4th methanol solution and is connected.
According to the device of recovering of vaporized hydrocarbons of the present utility model and extraction regenerated methanol, have that recovering of vaporized hydrocarbons rate is high, high, the lightweight oil of lightweight oil quality that reclaims and a low advantage of the mutual pollution level of methyl alcohol.Simultaneously owing to having separated out most lightweight oil in condensing steps and employing cold methanol washing absorption step, thus capacity load and the consumption of methanol extraction regeneration can be reduced, reduce efflux wastewater amount, reach energy-saving and cost-reducing object.
According to embodiments more of the present utility model, described condensation comprises: for carrying out the pre-cooler of first time cooling condensation to coal gas, and described pre-cooler has described first gas entry and the outlet of described cooled coal gas; Water cooler, described water cooler is connected for receiving the coal gas through condensation of once lowering the temperature of discharging from described pre-cooler and carrying out second time condensation to described coal gas with described pre-cooler; Separator, described separator is connected for receiving coal gas through second time condensation to isolate lightweight oil with described water cooler, described separator be connected with described pre-cooler with by described separator through twice cooling and the coal gas of separating out lightweight oil be drained in described pre-cooler and carry out cold recovery.
Preferably, the described pure methanol outlet of described methanol rectifying system is connected by the first water cooler with between described cold methanol entrance.
Preferably, the described water out of described methanol rectifying system is connected by the second water cooler with between described extraction water import.
Accompanying drawing explanation
Fig. 1 is the schema according to the recovering of vaporized hydrocarbons of the utility model embodiment and the method for extraction regenerated methanol;
Fig. 2 is the schematic diagram according to the recovering of vaporized hydrocarbons of the utility model embodiment and the device of extraction regenerated methanol;
Fig. 3 is according to the recovering of vaporized hydrocarbons of the utility model embodiment and the extraction device of regenerated methanol and the combination schematic diagram of low temperature washing device for methanol.
Embodiment
Be described below in detail embodiment of the present utility model, the example of described embodiment is shown in the drawings.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the utility model, and can not be interpreted as restriction of the present utility model.
Be described in detail according to the recovering of vaporized hydrocarbons of the utility model embodiment and the device 1000 of extraction regenerated methanol below with reference to Fig. 1-Fig. 3.Wherein be understandable that, can be used alone (as shown in Figure 2) according to the recovering of vaporized hydrocarbons of the utility model embodiment and the device 1000 of extraction regenerated methanol, can also combinationally use (as shown in Figure 3) with low temperature washing device for methanol 2000, what needs were described is, the structure of low temperature washing device for methanol 2000 can adopt structure of the prior art, low temperature washing device for methanol 2000 comprises tail gas washing tower 120, absorption tower 110, middle pressure flashing tower 130, carbonic acid gas washing tower 140, hydrogen sulphide concentration tower 150, the elements such as hot recycling tower 160 and methyl alcohol water tower 5, the principle of work etc. of low temperature washing device for methanol 2000 has been prior art, here be just not described in detail.
As shown in Figure 2, according to the device 1000 of the recovering of vaporized hydrocarbons of the utility model embodiment and extraction regenerated methanol, comprising: coal gas is carried out lowering the temperature the condensation of condensation, First Heat Exchanger 20, prewashing tower 30, flasher 40, second interchanger 50, extractor 60, azeotrope separation device 70 and methanol rectifying system 80.
Condensation comprises the first gas entry a for entering containing oil gas, cooled coal gas outlet b and the first lightweight oil outlet c, with pressure being drained into condensation from the first gas entry a containing oil gas of normal temperature carries out cooling condensation, in the process of cooling condensation, be condensed containing the lightweight oil in oil gas and water vapor, the lightweight oil of condensation and water vapor are isolated to obtain clean or white from coal gas, the coal gas of separating out lightweight oil is discharged from cooled coal gas outlet b, the clean or white of separating out is discharged from the first lightweight oil outlet c, not containing methyl alcohol in this strand of clean or white, purer lightweight oil can be obtained after oily water separation.
First Heat Exchanger 20 and cooled coal gas export b and are connected for receiving the coal gas after being separated of discharging from condensation, First Heat Exchanger 20 has cold de-oiling gas entry d and the first gas exit e, cold de-oiling coal gas is drained into First Heat Exchanger 20 from cold de-oiling gas entry d, the de-oiling coal gas of prewashing tower is adopted out to cool the coal gas in First Heat Exchanger 20, proper amount of methanol can be sprayed into simultaneously, all the other lightweight oils in coal gas and water vapor can be dissolved in cold methanol, thus while realizing the object to coal gas cooling, the pipeline of the lightweight oil blocking First Heat Exchanger 20 of separating out can be avoided.In concrete example of the present utility model, be sent to after generally coal gas being cooled to-10 DEG C ~-20 DEG C in prewashing tower 30.
Prewashing tower 30 comprises the second gas entry f, cold methanol entrance g, de-oiling gas exit h and the first methanol solution outlet i, second gas entry f is connected with the first gas exit e, de-oiling gas exit h be connected with cold de-oiling gas entry d discharge from First Heat Exchanger 20 be drained into prewashing tower 30 containing the coal gas of methanol solution from the second gas entry f, cold methanol is drained into prewashing tower 30 from cold methanol entrance g, cold methanol carries out washing absorption to coal gas, lightweight oil is thoroughly departed to obtain de-oiling coal gas from coal gas, de-oiling coal gas is discharged from de-oiling gas exit h, the methanol solution being mixed with lightweight oil discharges prewashing tower 30 from the first methanol solution outlet i.Wherein when recovering of vaporized hydrocarbons combinationally uses with low temperature washing device for methanol 2000 with the device 1000 of extraction regenerated methanol, prewashing tower 30 can be arranged at the bottom, absorption tower 110 in low temperature washing device for methanol 2000, prewashing tower 30 is directly connected by pipeline or riser with absorption tower 110, and cold methanol can from methyl alcohol rich solution at the bottom of methyl alcohol lean solution or absorption tower.
Flasher 40 has the first methanol solution entrance j, pneumatic outlet k and the second methanol solution outlet l, first methanol solution entrance j and the first methanol solution are exported i and are connected by the second interchanger 50, second interchanger 50 heats the methanol solution of discharging from the first methanol solution outlet i, that is, methanol solution after heating is drained into from the first methanol solution entrance j the precipitation carrying out gas flasher 40, the gas such as carbonic acid gas of separating out is discharged from pneumatic outlet k, the methanol solution of bubbing discharges flasher 40 from the second methanol solution outlet l, thus gas can be avoided to have an impact to follow-up extraction process.
Extractor 60 comprises the second methanol solution entrance m, extraction water import n, the second lightweight oil outlet o and the 3rd methanol solution outlet p, second methanol solution entrance m exports l with the second methanol solution and is connected, the methanol solution of discharging from flasher 40 is drained into extractor 60 from the second methanol solution entrance m, and water is drained into extractor 60 from extraction water import n.Utilize lightweight oil and water to the different dissolving power of methyl alcohol and density difference, after mixing stratification, obtain the less oil phase of density and the larger aqueous phase of density.The oil phase obtained after being separated is clean or white, and clean or white exports from the second lightweight oil.Send, the content of lightweight oil is about 90%-95%, and all the other are methyl alcohol and other impurity.The aqueous phase separated is discharged from the 3rd methanol solution outlet p.
Particularly, extraction tower can be vertical or horizontal container, horizontal container inside has the multi-cavity structure of the hybrid chamber of methanol solution and extraction water, layering chamber and disengagement chamber, and vertical vessel is liquid liquid counter-current extraction tower, adopts column internals to strengthen liquid liquid mixed effect and improves separating effect.In the figure 2 example, the second methanol solution entrance m and extraction water import n is same entrance.
Azeotrope separation device 70 comprises the 3rd methanol solution entrance q, the 3rd lightweight oil outlet r, the 4th methanol solution outlet s and non-condensable gas outlet t, and the 3rd methanol solution entrance q exports p with the 3rd methanol solution and is connected, and the 3rd lightweight oil outlet r is connected with the second methanol solution entrance m.Azeotrope separation device 70 utilizes the lightweight oil in the method methanol removal solution of organism azeotropic boiling point lowering and thermal rectification, in detach procedure, the non-condensable gas produced is discharged from non-condensable gas outlet t, in treating processes, lightweight oil is positioned at the surface of methanol solution, be mixed with water in lightweight oil due to precipitation, therefore the lightweight oil of this precipitation be expelled back in extractor 60 by the 3rd lightweight oil outlet r and the second methanol solution entrance m and carry out recovery extraction.The methanol solution having departed from lightweight oil discharges azeotrope separation device 70 from the 4th methanol solution outlet s.Wherein, azeotrope separation device 70 can adopt low-pressure steam or process waste as thermal source.
What wherein need to be described is, the concrete structure of azeotrope separation device 70 can adopt structure of the prior art, such as shown in Figure 2, azeotrope separation device 70 comprises the elements such as azeotrope column 4, reboiler 6a, water cooler 7a and the first separator 8a, the specific works step of azeotrope separation device 70, known by those skilled in the art, is just not described in detail here.
Methanol rectifying system 80 comprises the 4th methanol solution entrance u, pure methanol outlet v and water out w, and the 4th methanol solution entrance u exports s with the 4th methanol solution and is connected.The methanol solution of discharging from azeotrope separation device 70 is drained into methanol rectifying system 80 from the 4th methanol solution entrance u, methanol rectifying system 80 adopts method separation of methanol and the water of the different thermal rectification of boiling point, the water separated is discharged from water out w, and the pure methyl alcohol separated is discharged from pure methanol outlet v.Wherein, when recovering of vaporized hydrocarbons combinationally uses with low temperature washing device for methanol 2000 with the device 1000 of extraction regenerated methanol, methanol rectifying system 80 can be arranged separately, also can share with the methyl alcohol water tower 5 in low temperature washing device for methanol 2000.Wherein, methanol rectifying system 80 can adopt low-pressure steam or process waste as thermal source.
What wherein need to be described is, the concrete structure of methanol rectifying system 80 can adopt structure of the prior art, such as shown in Figure 2, methanol rectifying system 80 comprises the elements such as methyl alcohol water tower 5, reboiler 6b, water cooler 7b and the first separator 8b, the specific works step of methanol rectifying system 80, known by those skilled in the art, is just not described in detail here.
According to the device 1000 of the recovering of vaporized hydrocarbons of the utility model embodiment and extraction regenerated methanol operationally, first, the normal temperature coal gas with pressure be directly separated through cooling condensation from gasification or the normal temperature conversion coal gas with pressure be separated through cooling condensation from sulfur-resisting transformation device are drained into condensation from the first gas entry a and carry out condensation, most of lightweight oil in coal gas and water vapour are condensed precipitation, the clean or white of separating out is discharged from the first lightweight oil outlet c, and the coal gas of separating out lightweight oil is discharged from cooled coal gas outlet b.
The coal gas of discharging from condensation is drained into First Heat Exchanger 20, the de-oiling coal gas going out prewashing tower 30 is drained into First Heat Exchanger 20 from cold de-oiling gas entry d and cools coal gas, can spray into proper amount of methanol, cooled coal gas is drained into prewashing tower 30 from the first gas exit e and the second gas entry f simultaneously.
Cold methanol is drained into prewashing tower 30 from cold methanol entrance g and carries out washing absorption to coal gas, and the method for employing organic solvent physical absorption thoroughly removes the lightweight oil in coal gas.
The methanol solution of solution absorption lightweight oil, after the cold recovery of the second interchanger 50, is drained into from the first methanol solution entrance j precipitation carrying out gas flasher 40 and reclaims.The gas of separating out discharges flasher 40 from pneumatic outlet k.The methanol solution of bubbing is drained into from the second methanol solution outlet l and the second methanol solution entrance m the extraction regeneration carrying out methyl alcohol extractor 60.
Water is drained into extractor 60 from extraction water import n, utilizes lightweight oil and water to the different dissolving power of methyl alcohol and density difference, after mixing stratification, obtains the less oil phase of density and the larger aqueous phase of density.The oil phase obtained after being separated is clean or white and discharges from the second lightweight oil outlet o.Isolated aqueous phase is drained into azeotrope separation device 70 from the 3rd methanol solution outlet p and the 3rd methanol solution entrance q and departs from lightweight oil further.
Azeotrope separation device 70 adopts the lightweight oil in the thorough methanol removal solution of the method for organism azeotropic boiling point lowering and thermal rectification, the lightweight oil of tower top enrichment method is delivered to extractor 60 from the 3rd lightweight oil outlet r and is reclaimed, and methanol solution at the bottom of tower delivers to methanol rectifying system 80 from the 4th methanol solution outlet s and the 4th methanol solution entrance u.
Methanol rectifying system 80 adopts method separation of methanol and the water of the different thermal rectification of boiling point.The pure methyl alcohol of separating treatment is discharged from pure methanol outlet v, and the water separated is discharged from water out w.
Need to be described, the non-condensable gas that the flashed vapour from the pneumatic outlet k expellant gas, extractor 60 of flasher 40, azeotrope separation device 70 produce and the non-condensable gas that methanol rectifying system 80 produces can be sent to sulfur recovery system or low temperature washing device for methanol 2000 after collecting.
According to the device 1000 of the recovering of vaporized hydrocarbons of the utility model embodiment and extraction regenerated methanol, have that recovering of vaporized hydrocarbons rate lightweight oil quality that is high, that reclaim is high, lightweight oil and a low advantage of the mutual pollution level of methyl alcohol.Simultaneously owing to having separated out most lightweight oil in condensing steps and employing cold methanol washing absorption step, thus capacity load and the consumption of methanol extraction regeneration can be reduced, reduce efflux wastewater amount, reach energy-saving and cost-reducing object.
In preferred exemplary of the present utility model, the pure methanol outlet v of methanol rectifying system 80 is connected by the first water cooler 90 with between cold methanol entrance g.The water out w of methanol rectifying system 80 is connected by the second water cooler 100 with between extraction water import n.That is, the pure methyl alcohol of discharging from methanol rectifying system 80 is formed as cold methanol after the cooling of the first water cooler 90, and then cold methanol is drained into prewashing tower 30 from cold methanol entrance g and carries out washing absorption to coal gas.The water of discharging from methanol rectifying system 80 is drained into extractor 60 as extraction water after the cooling of the second water cooler 100.In brief, the methanol product that tower top obtains can be sent low temperature washing device for methanol 2000 back to or be circulated as prewashing methyl alcohol, return extractor 60 after water cooling at the bottom of tower as extraction water, superfluous water sends process after can cooling, and wherein in waste water, methanol content is about 100 ~ 500ppmw.Thus energy-saving and cost-reducing object can be reached.
Be understandable that, the pure methyl alcohol of discharging from the pure methanol outlet v of methanol rectifying system 80 also can be drained into First Heat Exchanger 20 as refrigerant after overcooling.
Preferably, in order to reduce energy consumption further, first water cooler 90 can carry out heat exchange with the second interchanger 50, that is, adopt the cold of the methanol solution of discharging from the first methanol solution outlet i of prewashing tower 30 to cool the methyl alcohol that the pure methanol outlet v from methanol rectifying system 80 discharges, adopt the heat of the methyl alcohol of discharging from the pure methanol outlet v of methanol rectifying system 80 to heat the methanol solution that the first methanol solution outlet i from prewashing tower 30 discharges.
The heat of the water of discharging from the water out w of methanol rectifying system 80 can be adopted in second water cooler 100 to heat the aqueous phase that the 3rd methanol solution outlet p from extractor 60 discharges, to reduce the heat of the water of discharging from water out w simultaneously.
According to embodiments more of the present utility model, condensation comprises: pre-cooler 2, water cooler 1 and separator 3, and wherein pre-cooler 2 to be lowered the temperature condensation for carrying out first time to coal gas, and pre-cooler 2 has the first gas entry a and cooled coal gas outlet b.Water cooler 1 is connected with pre-cooler 2 for receiving the coal gas through condensation of once lowering the temperature of discharging from pre-cooler 2 and carrying out second time condensation to coal gas.Separator 3 is connected for receiving coal gas through second time condensation to isolate lightweight oil with water cooler 1, separator 3 be connected with pre-cooler 2 with by separator 3 through twice cooling and the coal gas of separating out lightweight oil be drained in pre-cooler 2 and carry out cold recovery.
Specifically, the normal temperature coal gas with pressure be directly separated through cooling condensation from gasification or the normal temperature conversion coal gas with pressure about 40 degrees Celsius be separated through cooling condensation from sulfur-resisting transformation device, coal gas with pressure for normal temperature is drained in pre-cooler 2, coal gas is cooled to 20 degrees centigrade in pre-cooler 2, and lightweight oil wherein and water vapor are condensed; Then coal gas enters water cooler 1 and continues to be cooled to 5 degrees centigrade, and lightweight oil wherein and water vapor are condensed further, and the coal gas through twice condensation is separated in separator 3.Refrigerant provides cold in gas cooler 1, and temperature is about 0 degree Celsius; Battery limit (BL) sent by the lightweight oil separated from pre-cooler 2 and water cooler 1, not containing methyl alcohol in this strand of clean or white, can obtain purer clean or white after oily water separation.Coal gas in separator 3 after separation of lighter oil enters pre-cooler 2 and reclaims cold, re-heat to 30 degrees centigrade fed downstream.
Describe the method according to the recovering of vaporized hydrocarbons of the utility model embodiment and extraction regenerated methanol in detail below with reference to Fig. 1, utilize the method to may be used for processing the normal temperature coal gas with pressure be separated through cooling condensation from gasification or the normal temperature conversion coal gas with pressure be separated through cooling condensation from sulfur-resisting transformation device.The temperature of above-mentioned two kinds of coal gas is approximately 40 degrees Celsius.
As shown in Figure 1, comprise the steps: according to the recovering of vaporized hydrocarbons of the utility model embodiment and the method for extraction regenerated methanol
S1: carry out cooling condensation to isolate lightweight oil to containing oil gas, the refrigerant of about O DEG C wherein can be adopted to carry out cooling condensation to containing oil gas, that is, the normal temperature oil gas that contains with pressure is after the subcooling of refrigerant, major part lightweight oil and water vapour are condensed and separate out, thus can remove containing most lightweight oil in oil gas and water vapour, not containing methyl alcohol in the clean or white of separating out in this step, purer clean or white can be obtained after oily water separation.In brief, in this step, most of lightweight oil in the method condensation gas recovery reducing temperature is adopted.Particularly, the lightweight oil of about 80% can be reclaimed in this step.
S2: adopt out the de-oiling coal gas of prewashing tower will be cooled to design temperature through the condensed coal gas of cooling.
S3: be passed in cold methanol prewashing tower by being cooled to the coal gas of design temperature, cold methanol is adopted to carry out washing absorption to coal gas, remove the coal gas after lightweight oil to discharge from cold methanol prewashing tower, thus the object of the more thorough de-oiling to coal gas can be achieved, de-oiling coal gas can discharge to recycle.De-oiling gas temperature wherein owing to discharging from cold methanol prewashing tower is lower, is therefore used for cooling the coal gas in step S2 by the de-oiling coal gas of discharge.In other words, in this step, remaining lightweight oil in the method washing and recycling coal gas adopting organic solvent physical dissolution to absorb, and ensure in de-oiling coal gas hardly containing lightweight oil.Particularly, the typical operating temperature scope of washing process is-10 DEG C ~-20 DEG C.
S4: be drained into the precipitation carrying out gas in flasher after being heated by the methyl alcohol absorbing lightweight oil in step S3 and reclaim, thus the gas such as carbonic acid gas in methanol solution can be discharged, avoid the operation of gas to subsequent step to exert an adverse impact.Be understandable that, adopt the principle of type of heating and flasher bubbing known by those skilled in the art, be just not described in detail here.
S5: be drained into extractor carry out extracting to obtain oil phase and aqueous phase by water with from the methyl alcohol that flasher is discharged, specifically, utilize lightweight oil and water to the different dissolving power of methyl alcohol and density difference in this step, after mixing static layering, obtain the less oil phase of density and the larger aqueous phase of density, the oil phase drawn through separation is clean or white, sends as product.In brief, adopt the method for liquid-liquid extraction to realize being separated of lightweight oil and methyl alcohol in this step, and utilize density difference to realize being separated of oil phase and aqueous phase.Particularly, the content of the lightweight oil in oil phase is approximately 90%-95%, and all the other are methyl alcohol and other impurity, and the typical operating temperature of extraction is normal temperature.
S6: rectification process is carried out to isolate lightweight oil and methanol solution to the aqueous phase of discharging from step S5, isolated lightweight oil is expelled back in extractor and extracts, that is, utilize the lightweight oil in the method methanol removal solution of organism azeotropic boiling point lowering and thermal rectification in this step, in treating processes, lightweight oil is positioned at the surface of methanol solution, is mixed with water in the lightweight oil due to precipitation, is therefore expelled back in extractor by the lightweight oil of this precipitation and carries out recovery extraction.
S7: carry out rectification process to the methanol solution of discharging from step S6 and draw first alcohol and water to be separated, in other words, adopts method separation of methanol and the water of the different thermal rectification of boiling point in this step.
In summary, realize being separated of lightweight oil and methanol solution in step s 6, realize the separation of first alcohol and water in the step s 7, step S6 be all utilize the volatile difference of different substances to reach the object be separated in step S7.
In concrete example of the present utility model, methyl alcohol isolated in step S7 can be carried out cooling to obtain cold methanol, and the cold methanol obtained is passed in the cold methanol prewashing tower in step S3.In other words, the cold methanol adopted in step S3 can be that in step S7, isolated methyl alcohol draws after carrying out cooling.Thus can reduce costs.
Simultaneously can also by the extractor that is passed into after water cooling isolated in step S7 in step S5.In other words, the water be passed in step S5 in extractor can adopt separate out in step S7 through cooled water, thus the water yield in the external world that extractor needs to supplement can be reduced, reduce costs.
According to the recovering of vaporized hydrocarbons of the utility model embodiment and the method for extraction regenerated methanol, first by condensation and separation of containing the most of lightweight oil in oil gas, purer clean or white can be obtained.Then adopt cold methanol to separate out containing all the other lightweight oils in oil gas, thus can obtain not containing the de-oiling coal gas of lightweight oil.Adopt extracting process and rectificating method to isolate lightweight oil, first alcohol and water afterwards again, thus present method have that recovering of vaporized hydrocarbons rate is high, high, the lightweight oil of lightweight oil quality that reclaims and the low advantage of the mutual pollution level of methyl alcohol.Simultaneously owing to having separated out most lightweight oil in condensing steps and employing cold methanol washing absorption step, thus capacity load and the consumption of methanol extraction regeneration can be reduced, reduce efflux wastewater amount, reach energy-saving and cost-reducing object.
In concrete example of the present utility model, step S1 comprises following sub-step:
S11: will be passed in pre-cooler containing oil gas and carry out first time and to lower the temperature condensation;
S12: carry out second time to lower the temperature being passed in water cooler through the coal gas of first time cooling condensation in step S11 condensation, wherein refrigerant is passed into provide cold in water cooler, and the temperature of refrigerant is about 0 DEG C.
S13: be passed in separator by the coal gas through second time cooling condensation and carry out being separated to obtain lightweight oil, isolated coal gas enters in step S2 after being drained in pre-cooler and reclaiming cold and cools.That is, in pre-cooler for cool the normal temperature cold containing oil gas with pressure come since separator discharge through twice condensed coal gas, thus the consumption of refrigerant can be reduced.
Specifically, the normal temperature coal gas with pressure be directly separated through cooling condensation from gasification or the normal temperature conversion coal gas with pressure about 40 degrees Celsius be separated through cooling condensation from sulfur-resisting transformation device, coal gas with pressure for normal temperature is drained in pre-cooler, coal gas is cooled to 20 degrees centigrade in pre-cooler, and lightweight oil wherein and water vapor are condensed; Then coal gas enters water cooler and continues to be cooled to 5 degrees centigrade, and lightweight oil wherein and water vapor are condensed further, and the coal gas through twice condensation is separated in the separator.Refrigerant provides cold in water cooler, and temperature is about 0 degree Celsius; Battery limit (BL) sent by the lightweight oil separated from pre-cooler and water cooler, not containing methyl alcohol in this strand of clean or white, can obtain purer clean or white after oily water separation.Coal gas in the separator after separation of lighter oil enters pre-cooler and reclaims cold, re-heat to 30 degrees centigrade fed downstream.
In description of the present utility model, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise at least one this feature.In description of the present utility model, the implication of " multiple " is at least two, such as two, three etc., unless otherwise expressly limited specifically.
In the utility model, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection or each other can communication; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements, unless otherwise clear and definite restriction.For the ordinary skill in the art, the concrete meaning of above-mentioned term in the utility model can be understood as the case may be.
In the utility model, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present utility model or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and described embodiment of the present utility model above, be understandable that, above-described embodiment is exemplary, can not be interpreted as restriction of the present utility model, those of ordinary skill in the art can change above-described embodiment, revises, replace and modification in scope of the present utility model.
Claims (4)
1. a device for recovering of vaporized hydrocarbons and extraction regenerated methanol, is characterized in that, comprising:
Carry out to coal gas the condensation of condensation of lowering the temperature, described condensation comprises for entering containing the first gas entry of oil gas, cooled coal gas outlet and the outlet of the first lightweight oil;
First Heat Exchanger, described First Heat Exchanger and described cooled coal gas export and are connected for receiving the coal gas after being separated of discharging from described condensation, and described First Heat Exchanger has cold de-oiling gas entry and the first gas exit;
Prewashing tower, described prewashing tower comprises the outlet of the second gas entry, cold methanol entrance, de-oiling gas exit and the first methanol solution, and described second gas entry is connected with described first gas exit, and described de-oiling gas exit is connected with described cold de-oiling gas entry;
Flasher, described flasher has the outlet of the first methanol solution entrance, pneumatic outlet and the second methanol solution, described first methanol solution entrance is connected by the second interchanger between exporting with described first methanol solution, and described second interchanger heats the methanol solution of discharging from described first methanol solution outlet;
Extractor, described extractor comprises the second methanol solution entrance, extraction water import, the second lightweight oil outlet and the outlet of the 3rd methanol solution, and described second methanol solution entrance exports with described second methanol solution and is connected;
Azeotrope separation device, described azeotrope separation device comprises the 3rd methanol solution entrance, the 3rd lightweight oil outlet, the 4th methanol solution outlet and non-condensable gas outlet, described 3rd methanol solution entrance exports with described 3rd methanol solution and is connected, and described 3rd lightweight oil outlet is connected with described second methanol solution entrance;
Methanol rectifying system, described methanol rectifying system comprises the 4th methanol solution entrance, pure methanol outlet and water out, and described 4th methanol solution entrance exports with described 4th methanol solution and is connected.
2. the device of recovering of vaporized hydrocarbons according to claim 1 and extraction regenerated methanol, it is characterized in that, described condensation comprises:
For carrying out the pre-cooler of first time cooling condensation to coal gas, described pre-cooler has described first gas entry and the outlet of described cooled coal gas;
Water cooler, described water cooler is connected for receiving the coal gas through condensation of once lowering the temperature of discharging from described pre-cooler and carrying out second time condensation to described coal gas with described pre-cooler;
Separator, described separator is connected for receiving coal gas through second time condensation to isolate lightweight oil with described water cooler, described separator be connected with described pre-cooler with by described separator through twice cooling and the coal gas of separating out lightweight oil be drained in described pre-cooler and carry out cold recovery.
3. the device of recovering of vaporized hydrocarbons according to claim 1 and extraction regenerated methanol, it is characterized in that, the described pure methanol outlet of described methanol rectifying system is connected by the first water cooler with between described cold methanol entrance.
4. the device of recovering of vaporized hydrocarbons according to claim 1 and extraction regenerated methanol, it is characterized in that, the described water out of described methanol rectifying system is connected by the second water cooler with between described extraction water import.
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| CN201520071000.0U CN204455032U (en) | 2015-01-30 | 2015-01-30 | The device of recovering of vaporized hydrocarbons and extraction regenerated methanol |
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| CN201520071000.0U CN204455032U (en) | 2015-01-30 | 2015-01-30 | The device of recovering of vaporized hydrocarbons and extraction regenerated methanol |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104629817A (en) * | 2015-01-30 | 2015-05-20 | 上海鑫兴化工科技有限公司 | Method and device for recycling and extracting lightweight oil to regenerate methanol |
| CN106010673A (en) * | 2016-07-06 | 2016-10-12 | 山西潞安煤基合成油有限公司 | Method and device for preventing ammonia and organic sulfur accumulation in low temperature methanol washing system and removing device ammonium bicarbonate crystals |
| CN112322358A (en) * | 2020-10-22 | 2021-02-05 | 西南化工研究设计院有限公司 | System and method for removing and recovering tar and benzene hydrocarbon in raw gas |
-
2015
- 2015-01-30 CN CN201520071000.0U patent/CN204455032U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104629817A (en) * | 2015-01-30 | 2015-05-20 | 上海鑫兴化工科技有限公司 | Method and device for recycling and extracting lightweight oil to regenerate methanol |
| CN104629817B (en) * | 2015-01-30 | 2017-06-06 | 上海尧兴投资管理有限公司 | Light oil reclaims and extracts the method and device of regenerated methanol |
| CN106010673A (en) * | 2016-07-06 | 2016-10-12 | 山西潞安煤基合成油有限公司 | Method and device for preventing ammonia and organic sulfur accumulation in low temperature methanol washing system and removing device ammonium bicarbonate crystals |
| CN112322358A (en) * | 2020-10-22 | 2021-02-05 | 西南化工研究设计院有限公司 | System and method for removing and recovering tar and benzene hydrocarbon in raw gas |
| CN112322358B (en) * | 2020-10-22 | 2021-04-20 | 西南化工研究设计院有限公司 | System and method for removing and recovering tar and benzene hydrocarbon in raw gas |
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