CN203319963U - Device fore removing water and heavy hydrocarbon out of shale gas - Google Patents
Device fore removing water and heavy hydrocarbon out of shale gas Download PDFInfo
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- CN203319963U CN203319963U CN2013203265113U CN201320326511U CN203319963U CN 203319963 U CN203319963 U CN 203319963U CN 2013203265113 U CN2013203265113 U CN 2013203265113U CN 201320326511 U CN201320326511 U CN 201320326511U CN 203319963 U CN203319963 U CN 203319963U
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Abstract
The utility model relates to a device for removing water and heavy hydrocarbon out of shale gas. The device comprises a water and heavy hydrocarbon removal device, a triethylene glycol regeneration device and a heavy hydrocarbon treatment device; the water and heavy hydrocarbon removal device comprises two heat exchangers, a refrigerator and a three-phase separator; the triethylene glycol regeneration device comprises a regeneration tower, a heat exchanger and a gas-liquid separator; the heavy hydrocarbon treatment device comprises a dethanizing tower, a rectifying tower, a throttling device and a light oil cooler. By the device disclosed by the utility model, light components such as C1 and C2, as well as byproducts such as LPG (liquefied petroleum gas) and light oil are produced, the process route is advanced; the heat exchange route of cold and hot fluids is reasonable in design, and the reasonable match of cold quantity and heat quantity is realized, so that the energy consumption of the device is reduced as much as possible.
Description
Technical field
The utility model provides a kind of shale gas dehydration de-heavy hydrocarbon apparatus, from moisture, containing the shale gas of heavy hydrocarbon, removes moisture and heavy hydrocarbon, but also by-product liquefied petroleum gas (LPG) (LPG) and light oil products.
Background technology
Shale gas is exploitation Sweet natural gas out from shale bed, world's shale gas stock number is 457 tcms, suitable with the conventional gas stock number, and wherein shale gas technology mining resources amount is 187 tcms, economic worth is huge, has very large development potentiality.At present, the exploitation of China's shale gas is in gas reservoir exploration and preliminary exploitation pilot phase.By in April, 2012, China determines 33 shale gas Favorable Areas altogether, 58 mouthfuls of shale gas completions, and wherein horizontal well is 15 mouthfuls.Along with the shale gas exploration right is progressively open to the public, the shale gas exploitation of Future Ten year will be expected to be rapidly developed.Shale gas is as an emerging unconventional energy resource, and its treatment technology is also relatively less, along with the exploitation of new forms of energy, the development requirement of the treatment technology of shale gas is also increased day by day.The utility model proposes a kind for the treatment of technology of shale gas, for purifying shale gas, reclaim light constituent.
Triethylene glycol, have another name called triglycol, is colourless, odorless, pleasantly sweet thickness, transparent or micro-band yellow liquid; Relative density is 1.126, and boiling point is 285 ℃, and fusing point is-7 ℃, flammable, and flash-point is 176.7 ℃, and spontaneous ignition temperature is 371 ℃, can be miscible with any ratio with water, can reduce the freezing point of water, and great water absorbability is arranged.Skeleton symbol is HO-(CH2) 2-O-(CH2) 2-O-(CH2) 2-OH, and molecular formula is C6H14O4; Relative molecular weight is 150.2, and its key technical indexes is: acidity (with acetometer)≤100mg/kg, density (20 ℃) is 1.1215-1.1245g/cm3.Triglycol dehydration belongs to the solvent absorbing dehydration, be utilize the triglycol solvent under high normal pressure and temperature by the moisture absorption in Sweet natural gas or synthetic gas, and, in the situation that step-down and intensification are deviate from water from solvent, triglycol obtains regeneration simultaneously.
The utility model content
The utility model provides a kind of shale gas dehydration de-heavy hydrocarbon treatment unit.
Device of the present utility model comprises: dehydration de-heavy hydrocarbon apparatus, triglycol regenerating unit and heavy hydrocarbon treatment unit;
The dehydration de-heavy hydrocarbon apparatus comprises First Heat Exchanger, the second interchanger, a refrigerator and a triphase separator;
The triglycol regenerating unit comprises a regenerator column, the 3rd interchanger, a gas-liquid separator;
The heavy hydrocarbon treatment unit comprises a deethanizing column, a rectifying tower, a throttling set and a light oil water cooler;
Wherein, described First Heat Exchanger comprises a mixed phase access road, a mixed phase exit passageway, a light constituent access road and a light constituent exit passageway;
Described the second interchanger comprises a mixed phase access road, a mixed phase exit passageway, a heavy constituent access road and a heavy constituent exit passageway;
Described refrigerator comprises a process fluid access road and a process fluid exit passageway;
Described triphase separator comprises a mixed phase access road, a top gaseous phase outlet passage, a heavy constituent exit passageway and a bottom triglycol exit passageway;
Described regenerator column comprises a triglycol centre entrance passage, a triglycol outlet at bottom passage and a steam outlet passage;
Described the 3rd interchanger comprises a triglycol access road, a triglycol exit passageway, a rich triglycol access road and a rich triglycol exit passageway;
Described gas-liquid separator comprises a triglycol access road, a triglycol exit passageway and a steam outlet passage;
Described deethanizing column comprises a heavy constituent access road, a light constituent top exit passage and a heavy constituent outlet at bottom passage;
Described rectifying tower comprises a heavy constituent access road, a gaseous phase outlet passage and a light oil exit passageway;
Described light oil water cooler comprises a light oil access road and a light oil exit passageway;
Wherein, the mixed phase exit passageway of First Heat Exchanger connects the mixed phase access road of the second interchanger, the mixed phase exit passageway of the second interchanger connects the process fluid access road of refrigerator, and the process fluid exit passageway of refrigerator connects the mixed phase access road of triphase separator; The top gaseous phase outlet passage of triphase separator connects the light constituent access road of First Heat Exchanger; The heavy constituent exit passageway of triphase separator connects the heavy constituent access road of the second interchanger, and the heavy constituent exit passageway of the second interchanger is connected to the heavy constituent access road of deethanizing column; The bottom triglycol exit passageway of triphase separator is connected to the rich triglycol access road of the 3rd interchanger, the rich triglycol exit passageway of the 3rd interchanger is connected to the triglycol access road of gas-liquid separator, and the triglycol exit passageway of gas-liquid separator is connected to the triglycol centre entrance passage of regenerator column; The triglycol outlet at bottom passage of described regenerator column is connected to the triglycol access road of described the 3rd interchanger, and the triglycol exit passageway of the 3rd interchanger is connected to the access road of First Heat Exchanger via the triglycol pump; After converging, the top gaseous phase outlet passage of the light constituent top exit passage of described deethanizing column and described triphase separator is connected to the light constituent access road of First Heat Exchanger, the heavy constituent outlet at bottom passage of deethanizing column is connected to the heavy constituent access road of rectifying tower via throttling set, the light oil exit passageway of rectifying tower is connected to the light oil access road of light oil water cooler.
Preferably, described regenerator column is provided with the trim the top of column system, this return-flow system comprises overhead condenser, regenerator column return tank and pump, described overhead condenser comprises a triglycol access road, a triglycol exit passageway, a steam entry passage, a steam outlet passage, the triglycol access road of overhead condenser is connected with the bottom triglycol exit passageway of triphase separator, the triglycol exit passageway of overhead condenser is connected with the triglycol access road of the 3rd interchanger, the steam entry passage of overhead condenser is connected with the steam outlet passage of regenerator column, the steam outlet passage of overhead condenser is connected with the access road of regenerator column return tank, the first exit passageway of regenerator column return tank is connected with the reflux inlet passage of regenerator column via pump, the second exit passageway is as the steam outlet passage.
Preferably, described deethanizing column is provided with the trim the top of column system, comprise an overhead condenser, a deethanizing column return tank, a reflux pump, the light constituent top exit passage of deethanizing column is connected with the entrance of overhead condenser, the outlet of overhead condenser is connected with the entrance of deethanizing column return tank, the first outlet of deethanizing column return tank is connected with the reflux inlet of deethanizing column via reflux pump, and the second outlet of deethanizing column return tank is connected to the light constituent access road of First Heat Exchanger after converging with the top gaseous phase outlet passage of described triphase separator.
Preferably, described rectifying tower is provided with the trim the top of column system, comprise an overhead condenser, a rectifying tower return tank, a reflux pump, the gaseous phase outlet passage of rectifying tower is connected with the entrance of overhead condenser, the outlet of overhead condenser is connected with the entrance of rectifying tower return tank, the first outlet of rectifying tower return tank is connected with the reflux inlet of rectifying tower via reflux pump, and the second outlet of rectifying tower return tank is as the liquefied petroleum gas (LPG) exit passageway.
Preferably, adopt the reboiler of built-in, autoclave or heat siphon type at the bottom of the tower of regenerator column, deethanizing column and rectifying tower.
Use the method for device of the present utility model to comprise the de-heavy hydrocarbon operation of dehydration and heavy hydrocarbon treatment process two portions; The de-heavy hydrocarbon operation of dehydration comprise by shale gas with carry out subzero treatment after triglycol mixes, then enter in triphase separator and be separated into triglycol, light constituent and the heavy constituent that has absorbed moisture, the triglycol that has wherein absorbed moisture is regenerated in regenerator column, light constituent is as outside product discharge system, and heavy constituent enters the heavy hydrocarbon treatment process; Described heavy hydrocarbon treatment process comprises that isolated heavy constituent in the de-heavy hydrocarbon operation of dehydration is carried out to stripping in deethanizing column further isolates light constituent and heavy constituent, outside wherein light constituent is exhausted from system as product, wherein heavy constituent enters in rectifying tower and isolates light oil and isolate gas phase, and this gas phase is cooled into liquefied petroleum gas (LPG).
In the de-heavy hydrocarbon operation of described dehydration, from the triglycol that completes regeneration of triglycol regenerating unit with after the raw material shale gas mixes, enter together First Heat Exchanger, with the light constituent heat exchange such as isolated C1 and C2 in shale gas from triphase separator, then enter the second interchanger, with the above heavy constituent heat exchange of isolated C3 in shale gas from triphase separator, after reclaiming cold with above-mentioned First Heat Exchanger and the second interchanger heat exchange respectively, enter refrigerator, be cooled to approximately-20 ℃～-40 ℃ (preferably-25 ℃～-35 ℃ through refrigerator, or-28 ℃～-32 ℃, more preferably be cooled to approximately-30 ℃), in the process of cooling gradually, triglycol and shale gas fully mix and shale gas in moisture by triglycol, absorbed gradually, enter afterwards in triphase separator, absorbed the triglycol of moisture, the light constituents such as the C1 in shale gas and C2, in shale gas, the above heavy constituent of C3 is separated into three-phase, the light constituent such as C1 and C2 goes the First Heat Exchanger heat exchange through triphase separator top gas phase channel, temperature rises to normal temperature, be the product that has removed moisture and heavy hydrocarbon, the above heavy constituent of C3 is gone the second interchanger heat exchange through triphase separator bottom hydrocarbon exit passageway, and heat exchange is to approximately-10-10 ℃, duplicate removal hydrocarbon treatment unit after preferably-5-5 ℃, the triglycol exit passageway of triglycol through the triphase separator bottom that has absorbed moisture removes the triglycol regenerating unit.
Describedly through the isolated triglycol that has absorbed moisture of triphase separator, at first enter the regenerator column overhead condenser, for overhead condenser provides cold, self be increased to-30--20 of temperature ℃ (preferably-27--23 ℃), then enter the 3rd interchanger (or described through the isolated triglycol that has absorbed moisture of triphase separator, directly enter the 3rd interchanger) with from the triglycol heat exchange that completes regeneration at the bottom of regenerator column, temperature is increased to 150-180 ℃ (preferably 160～170 ℃), then entering gas-liquid separator separates is gas-liquid two-phase, the gas phase overwhelming majority that gas-liquid separator separates goes out is water vapor, isolated liquid phase enters in regenerator column the moisture water vapor of isolating in triglycol and separates from the regenerator column tower top, the regenerator column working pressure is 0.1-0.2MPaG, the triglycol that completes regeneration that regenerator column bottom obtains enters the 3rd interchanger heat exchange, and be down to-10-10 of temperature ℃ (preferably-5-5 ℃) then is pumped to the entrance of described First Heat Exchanger through triglycol.Preferably, the isolated gas phase of regeneration overhead section enters the regeneration overhead condenser and is cooled to for example 90-130 ℃, then enter separatory in the regeneration overhead return tank, isolated liquid phase is sent back in regenerator column through regenerator reflux pump as refluxing after going out the bottom liquid phases exit passageway of regeneration overhead return tank, and the gas phase that the regeneration overhead return tank separates is that water vapor separates from regeneration overhead return tank gaseous phase outlet passage.
In described heavy hydrocarbon treatment process, the heavy constituent more than the described C3 that completes heat exchange in the second interchanger removes the wherein remaining light constituents such as C1, C2 in entering deethanizing column, and the deethanizing column working pressure is 2.0-5.0MPaG; The isolated liquid phase in deethanizing column bottom, i.e. the above heavy constituent throttling of C3 enters in rectifying tower to 1.0-2.0MPaG.
Preferably, the isolated gas phase in deethanizing column top enters for example be cooled to-40--15 ℃ of (preferably-35--20 ℃ in deethanizing tower top condenser, more preferably-30--25 ℃), then enter separatory in deethanizing tower top return tank, isolated liquid phase is sent back in deethanizing column through the deethanizing column reflux pump as trim the top of column, and the gas phase that deethanizing tower top return tank separates is that the light constituents such as C1, C2 converge in the isolated gas phase in triphase separator top in the de-heavy hydrocarbon operation of described dehydration.
Preferably, at first the gas phase at rectifying tower top enters and enter the rectifying tower top return tank after the rectifying tower top condenser is cooled to liquid phase, and Partial Liquid Phase is delivered to rectifying tower as trim the top of column through the rectifying tower reflux pump, and the part extraction is liquefied petroleum gas (LPG) (LPG) product; Isolate the above heavy constituent of C5 from rectifier bottoms, after the light oil water cooler is cooled to normal temperature, be light oil products.
Can adopt the reboiler of pattern arbitrarily such as built-in, autoclave, heat siphon type at the bottom of the tower of regenerator column, deethanizing column and rectifying tower.
Here, pressure unit MPaG is MPa, gauge pressure.
Described light constituent main (for example, more than 50wt%, preferably more than 60wt%, more preferably more than 70wt%, more preferably more than 90wt%, more preferably more than 95wt%) is C1, C2 hydrocarbon.Described heavy constituent main (for example, more than 50wt%, preferably more than 60wt%, more preferably more than 70wt%, more preferably more than 90wt%, more preferably more than 95wt%) is the above hydrocarbon of C3, for example C3, C4, C5, C6, C6+ hydrocarbon.Wherein C1, C2, C3, C4, C5, C6 philosophy mean the hydro carbons (comprising alkane, alkene and aromatic hydrocarbons) of corresponding carbonatoms.C3 in the application
+Refer to containing three and three hydro carbons (or paraffinic) that carbonatoms is above.
Advantage of the present utility model:
1, device of the present utility model adopts the brand-new de-heavy hydrocarbon method of shale gas dehydration, the light constituents such as C1, C2 is separated and heavy constituent is processed and reclaimed, and obtains LPG and light oil byproduct, economic and reliable.Shale gas dew points at normal pressure after the de-heavy hydrocarbon of dehydration is down to≤and-76 ℃, for example be removed to≤150ppm of heavy hydrocarbon component that C6 and C6 are above, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
2, cold and hot fluid heat exchange highway route design is reasonable, realizes the rational Match of fluid cold, heat, makes the plant energy consumption reduce;
3, the more traditional triglycol method of dewatering dehydration route is simple, more easy to operate, significantly reduces costs.
The accompanying drawing explanation
Fig. 1 is the de-heavy hydrocarbon process device figure of shale gas dehydration described in the utility model.
E1, First Heat Exchanger E2, the second interchanger E3, the 3rd interchanger E4, regeneration overhead condenser E5, light oil water cooler E6, deethanizing tower top condenser E7, rectifying tower top condenser E8, deethanizing column reboiler E9, rectifying tower reboiler E10, regenerator column reboiler G1, regeneration overhead return tank G2, deethanizing tower top return tank G3, rectifying tower top return tank RP1, regenerator reflux pump RP2, deethanizing column reflux pump RP3, rectifying tower reflux pump X1, refrigerator V1, triphase separator V2, gas-liquid separator T1, regenerator column T2, deethanizing column T3, rectifying tower P1, triglycol pump V-1, throttling set
Embodiment
The utility model provides a kind of shale gas dehydration de-heavy hydrocarbon treatment unit.
Device of the present utility model comprises: dehydration de-heavy hydrocarbon apparatus, triglycol regenerating unit and heavy hydrocarbon treatment unit;
The dehydration de-heavy hydrocarbon apparatus comprises First Heat Exchanger E1, the second interchanger E2, a refrigerator X1 and a triphase separator V1;
The triglycol regenerating unit comprises a regenerator column T1, the 3rd interchanger E4, a gas-liquid separator V2 and a triglycol pump P1, wherein said regenerator column T1 is provided with trim the top of column system and tower bottom reboiler E10, and this return-flow system comprises an overhead condenser E4 who is connected with regenerator column T1, return tank of top of the tower G1, a reflux pump RP1;
The heavy hydrocarbon treatment unit comprises a deethanizing column T2, rectifying tower T3, a throttling set V-1 and a light oil water cooler E5, wherein said deethanizing column T2 is provided with trim the top of column system and a reboiler E8, and this return-flow system comprises an overhead condenser E6 who is connected with deethanizing column T2, return tank of top of the tower G2, a reflux pump RP2; Described rectifying tower T3 is provided with trim the top of column system and a tower bottom reboiler E9, and this return-flow system comprises an overhead condenser E7 who is connected with rectifying tower T3, return tank of top of the tower G3, a reflux pump RP3;
Wherein, described First Heat Exchanger E1 comprises a mixed phase access road, a mixed phase exit passageway, a light constituent access road and a light constituent exit passageway;
Described the second interchanger E2 comprises a mixed phase access road, a mixed phase exit passageway, a heavy constituent access road and a heavy constituent exit passageway;
Described refrigerator X1 comprises a process fluid access road and a process fluid exit passageway;
Described triphase separator V1 comprises a mixed phase access road, a top gaseous phase outlet passage, a heavy constituent exit passageway and a bottom triglycol exit passageway;
Described regenerator column T1 comprises a triglycol centre entrance passage, a triglycol outlet at bottom passage and a steam outlet passage;
Described the 3rd interchanger E3 comprises a triglycol access road, a triglycol exit passageway, a rich glycol access road and a rich glycol exit passageway;
Described gas-liquid separator V2 comprises a triglycol access road, a triglycol exit passageway and a steam outlet passage;
Described deethanizing column T2 comprises a heavy constituent access road, a light constituent top exit passage and a heavy constituent outlet at bottom passage;
Described rectifying tower T3 comprises a heavy constituent access road, a LPG exit passageway and a light oil exit passageway;
Described light oil water cooler E5 comprises a light oil access road and a light oil exit passageway;
Wherein, the mixed phase exit passageway of First Heat Exchanger E1 connects the mixed phase access road of the second interchanger E2, the mixed phase exit passageway of the second interchanger E2 connects the process fluid access road of refrigerator X1, and the process fluid exit passageway of refrigerator X1 connects the mixed phase access road of triphase separator V1; The top gaseous phase outlet passage of triphase separator V1 connects the light constituent access road of First Heat Exchanger E1; The heavy constituent exit passageway of triphase separator V1 connects the heavy constituent access road of the second interchanger E2, and the heavy constituent exit passageway of the second interchanger E2 is connected to the heavy constituent access road of deethanizing column T2; The bottom triglycol exit passageway of triphase separator V1 is connected to the triglycol access road of the overhead condenser E4 of regenerator column T1, the steam entry passage of overhead condenser E4 is connected with the steam outlet passage of regenerator column T1, the steam outlet passage of overhead condenser E4 is connected with the access road of regenerator column return tank, the first exit passageway of regenerator column return tank is connected with the reflux inlet passage of regenerator column via pump, and the second exit passageway is as the steam outlet passage.The triglycol top exit passage of the overhead condenser E4 of regenerator column T1 is connected to the rich triglycol access road of the 3rd interchanger E3, the rich triglycol exit passageway of the 3rd interchanger E3 is connected to the triglycol access road of gas-liquid separator V2, and the triglycol exit passageway of gas-liquid separator V2 is connected to the triglycol centre entrance passage of regenerator column T1; The triglycol outlet at bottom passage of described regenerator column T1 is connected to the triglycol access road of described the 3rd interchanger E3, and the triglycol exit passageway of the 3rd interchanger E3 is connected to the access road of First Heat Exchanger E1 via triglycol pump P1.
The light constituent top exit passage of deethanizing column T2 is connected to the access road of deethanizing column return tank G2 via overhead condenser E6, after converging, the top gaseous phase outlet passage of return tank G2 top gaseous phase outlet passage and described triphase separator V1 is connected to the light constituent access road of First Heat Exchanger E1, the heavy constituent outlet at bottom passage of deethanizing column T2 is connected to the heavy constituent access road of rectifying tower T3 via throttling set V-1, the light oil exit passageway of rectifying tower T3 is connected to the light oil access road of light oil water cooler E5.The top gaseous phase outlet passage of rectifying tower T3 is connected to the access road of rectifying tower return tank G3 via overhead condenser E7, one of them liquid-phase outlet passage of return tank G3 is connected with the liquefied petroleum gas product storage tank, another liquid-phase outlet passage, via reflux pump RP3, is connected to the reflux inlet passage of rectifying tower T3.
Use the method for device of the present utility model to comprise the de-heavy hydrocarbon operation of dehydration and heavy hydrocarbon treatment process two portions; The de-heavy hydrocarbon operation of dehydration comprise adopt triglycol low temperature in triphase separator V1 remove shale gas in moisture and heavy hydrocarbon, the triglycol that has absorbed moisture is regenerated in regenerator column T1; The heavy hydrocarbon treatment process comprises that in shale gas, the above heavy constituent of C3 is isolated the light constituents such as remaining C1, C2 in deethanizing column T2, and the above heavy constituent of C3 enters in rectifying tower T3 and is separated into LPG and light oil.
With reference to accompanying drawing 1, in the de-heavy hydrocarbon operation of described dehydration, from the triglycol that completes regeneration of triglycol regenerating unit with after the raw material shale gas mixes, enter together First Heat Exchanger E1, with the light constituent heat exchange such as isolated C1 and C2 in shale gas from triphase separator V1, then enter the second interchanger E2, with the above heavy constituent heat exchange of isolated C3 in shale gas from triphase separator V1, after reclaiming cold with above-mentioned First Heat Exchanger E1 and the second interchanger E2 heat exchange respectively, enter refrigerator X1, be cooled to approximately-30 ℃ through refrigerator X1, in the process of cooling gradually, triglycol and shale gas fully mix and shale gas in moisture by triglycol, absorbed gradually, enter afterwards in triphase separator V1, absorbed the triglycol of moisture, the light constituents such as the C1 in shale gas and C2, in shale gas, the above heavy constituent of C3 is separated into three-phase, the light constituent such as C1 and C2 goes First Heat Exchanger E1 heat exchange through triphase separator V1 top gas phase channel, temperature rises to normal temperature, be the product that has removed moisture and heavy hydrocarbon, the above heavy constituent of C3 is gone the second interchanger E2 heat exchange through triphase separator V1 bottom hydrocarbon exit passageway, and heat exchange is to duplicate removal hydrocarbon treatment unit after approximately-10-10 ℃, the triglycol exit passageway of triglycol through triphase separator V1 bottom that has absorbed moisture removes the triglycol regenerating unit.
Comprise the triglycol step for regeneration in the de-heavy hydrocarbon operation of described dehydration, in the triglycol step for regeneration, describedly through the isolated triglycol that has absorbed moisture of triphase separator V1, at first enter regenerator column T1 overhead condenser E4, for overhead condenser, E4 provides cold, self be increased to-30--20 ℃ of temperature, then enter the 3rd interchanger E3 with from the triglycol heat exchange that completes regeneration at the bottom of regenerator column T1 tower, temperature is increased to 150-180 ℃, then enter gas-liquid separator V2 and be separated into gas-liquid two-phase, the isolated gas phase of gas-liquid separator V1 is discharged, its overwhelming majority is water vapor, isolated liquid phase enters regenerator column T1, regenerator column T1 working pressure is 0.1-0.2MPaG, the isolated gas phase in regenerator column T1 top enters regeneration overhead condenser E4 and is cooled to for example 90-130 ℃, then enter separatory in regeneration overhead return tank G1, isolated liquid phase is sent back in regenerator column T1 through regenerator reflux pump RP1 as refluxing after going out the bottom liquid phases exit passageway of regeneration overhead return tank G1, and the gas phase that regeneration overhead return tank G1 separates is that water vapor separates from regeneration overhead return tank G1 gaseous phase outlet passage, the triglycol that completes regeneration that regenerator column T1 bottom obtains enters the 3rd interchanger E3 heat exchange, and then be down to-10-10 ℃ of temperature delivers to the entrance of described First Heat Exchanger through triglycol pump P1.
In described heavy hydrocarbon treatment process, the heavy constituent more than the described C3 that completes heat exchange in the second interchanger E2 removes the wherein remaining light constituents such as C1, C2 in entering deethanizing column T2, and deethanizing column T2 working pressure is 2.0-5.0MPaG; The isolated gas phase in deethanizing column T2 top enters for example be cooled to-40--15 ℃ in deethanizing tower top condenser E6, then enter separatory in deethanizing tower top return tank G2, the liquid phase separated is sent back in deethanizing column T2 through deethanizing column reflux pump RP2 as trim the top of column, and the gas phase that deethanizing tower top return tank G2 separates is that the light constituents such as C1, C2 converge in the isolated gas phase in triphase separator V1 top in the de-heavy hydrocarbon operation of described dehydration; The isolated liquid phase in deethanizing column T2 bottom, be that the above heavy constituent throttling of C3 enters in rectifying tower T3 to 1.0-2.0MPaG, at first the gas phase at rectifying tower T3 top enters and enter rectifying tower top return tank G3 after rectifying tower top condenser E7 is cooled to liquid phase, Partial Liquid Phase is delivered to rectifying tower T3 as trim the top of column through rectifying tower reflux pump RP3, the part extraction, be the LPG product; Isolate the above heavy constituent of C5 from rectifying tower T3 bottom, after light oil water cooler E5 is cooled to normal temperature, be light oil products.
Can adopt the reboiler of pattern arbitrarily such as built-in, autoclave, heat siphon type at the bottom of the tower of regenerator column T1, deethanizing column T2 and rectifying tower T3.Shale gas dew points at normal pressure after the de-heavy hydrocarbon of dehydration is down to≤and-76 ℃, the above heavy hydrocarbon component of C6 and C6 is removed to the soluble degree of LNG, for example≤150ppm, preferably≤100ppm, more preferably≤80ppm, more preferably≤50ppm.
Here, pressure unit MPaG is MPa, gauge pressure.
Claims (5)
1. a shale gas dehydration takes off the heavy hydrocarbon treatment unit, and it is characterized in that: this device comprises: dehydration de-heavy hydrocarbon apparatus, triglycol regenerating unit and heavy hydrocarbon treatment unit;
The dehydration de-heavy hydrocarbon apparatus comprises First Heat Exchanger, the second interchanger, a refrigerator and a triphase separator;
The triglycol regenerating unit comprises a regenerator column, the 3rd interchanger, a gas-liquid separator;
The heavy hydrocarbon treatment unit comprises a deethanizing column, a rectifying tower, a throttling set and a light oil water cooler;
Wherein, described First Heat Exchanger comprises a mixed phase access road, a mixed phase exit passageway, a light constituent access road and a light constituent exit passageway;
Described the second interchanger comprises a mixed phase access road, a mixed phase exit passageway, a heavy constituent access road and a heavy constituent exit passageway;
Described refrigerator comprises a process fluid access road and a process fluid exit passageway;
Described triphase separator comprises a mixed phase access road, a top gaseous phase outlet passage, a heavy constituent exit passageway and a bottom triglycol exit passageway;
Described regenerator column comprises a triglycol centre entrance passage, a triglycol outlet at bottom passage and a steam outlet passage;
Described the 3rd interchanger comprises a triglycol access road, a triglycol exit passageway, a rich triglycol access road and a rich triglycol exit passageway;
Described gas-liquid separator comprises a triglycol access road, a triglycol exit passageway and a steam outlet passage;
Described deethanizing column comprises a heavy constituent access road, a light constituent top exit passage and a heavy constituent outlet at bottom passage;
Described rectifying tower comprises a heavy constituent access road, a gaseous phase outlet passage and a light oil exit passageway;
Described light oil water cooler comprises a light oil access road and a light oil exit passageway;
Wherein, the mixed phase exit passageway of First Heat Exchanger connects the mixed phase access road of the second interchanger, the mixed phase exit passageway of the second interchanger connects the process fluid access road of refrigerator, and the process fluid exit passageway of refrigerator connects the mixed phase access road of triphase separator; The top gaseous phase outlet passage of triphase separator connects the light constituent access road of First Heat Exchanger; The heavy constituent exit passageway of triphase separator connects the heavy constituent access road of the second interchanger, and the heavy constituent exit passageway of the second interchanger is connected to the heavy constituent access road of deethanizing column; The bottom triglycol exit passageway of triphase separator is connected to the rich triglycol access road of the 3rd interchanger, the rich triglycol exit passageway of the 3rd interchanger is connected to the triglycol access road of gas-liquid separator, and the triglycol exit passageway of gas-liquid separator is connected to the triglycol centre entrance passage of regenerator column; The triglycol outlet at bottom passage of described regenerator column is connected to the triglycol access road of described the 3rd interchanger, and the triglycol exit passageway of the 3rd interchanger is connected to the access road of First Heat Exchanger via the triglycol pump; After converging, the top gaseous phase outlet passage of the light constituent top exit passage of described deethanizing column and described triphase separator is connected to the light constituent access road of First Heat Exchanger, the heavy constituent outlet at bottom passage of deethanizing column is connected to the heavy constituent access road of rectifying tower via throttling set, the light oil exit passageway of rectifying tower is connected to the light oil access road of light oil water cooler.
2. according to the device of claim 1, it is characterized in that: described regenerator column is provided with the trim the top of column system, this return-flow system comprises overhead condenser, regenerator column return tank and pump, described overhead condenser comprises a triglycol access road, a triglycol exit passageway, a steam entry passage, a steam outlet passage, the triglycol access road of overhead condenser is connected with the bottom triglycol exit passageway of triphase separator, the triglycol exit passageway of overhead condenser is connected with the triglycol access road of the 3rd interchanger, the steam entry passage of overhead condenser is connected with the steam outlet passage of regenerator column, the steam outlet passage of overhead condenser is connected with the access road of regenerator column return tank, the first exit passageway of regenerator column return tank is connected with the reflux inlet passage of regenerator column via pump, the second exit passageway is as the steam outlet passage.
3. according to the device of claim 1 or 2, it is characterized in that: described deethanizing column is provided with the trim the top of column system, comprise an overhead condenser, a deethanizing column return tank, a reflux pump, the light constituent top exit passage of deethanizing column is connected with the entrance of overhead condenser, the outlet of overhead condenser is connected with the entrance of deethanizing column return tank, the first outlet of deethanizing column return tank is connected with the reflux inlet of deethanizing column via reflux pump, the second outlet of deethanizing column return tank is connected to the light constituent access road of First Heat Exchanger after converging with the top gaseous phase outlet passage of described triphase separator.
4. according to the device of claim 1 or 2, it is characterized in that: described rectifying tower is provided with the trim the top of column system, comprise an overhead condenser, a rectifying tower return tank, a reflux pump, the gaseous phase outlet passage of rectifying tower is connected with the entrance of overhead condenser, the outlet of overhead condenser is connected with the entrance of rectifying tower return tank, the first outlet of rectifying tower return tank is connected with the reflux inlet of rectifying tower via reflux pump, and the second outlet of rectifying tower return tank is as the liquefied petroleum gas (LPG) exit passageway.
5. device according to claim 1 and 2 is characterized in that: the reboiler that adopts built-in, autoclave or heat siphon type at the bottom of the tower of regenerator column, deethanizing column and rectifying tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203265113U CN203319963U (en) | 2013-06-07 | 2013-06-07 | Device fore removing water and heavy hydrocarbon out of shale gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013203265113U CN203319963U (en) | 2013-06-07 | 2013-06-07 | Device fore removing water and heavy hydrocarbon out of shale gas |
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| Publication Number | Publication Date |
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| CN203319963U true CN203319963U (en) | 2013-12-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013203265113U Expired - Fee Related CN203319963U (en) | 2013-06-07 | 2013-06-07 | Device fore removing water and heavy hydrocarbon out of shale gas |
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| Country | Link |
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| CN (1) | CN203319963U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103351895A (en) * | 2013-06-07 | 2013-10-16 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN105038890A (en) * | 2015-06-30 | 2015-11-11 | 柳州市山泰气体有限公司 | Separation method for preparing liquefied petroleum gas (LPG) from high-temperature gas synthesis gas |
-
2013
- 2013-06-07 CN CN2013203265113U patent/CN203319963U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103351895A (en) * | 2013-06-07 | 2013-10-16 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN103351895B (en) * | 2013-06-07 | 2015-05-06 | 新地能源工程技术有限公司 | Method and device for removing water and heavy hydrocarbons from shale gas |
| CN105038890A (en) * | 2015-06-30 | 2015-11-11 | 柳州市山泰气体有限公司 | Separation method for preparing liquefied petroleum gas (LPG) from high-temperature gas synthesis gas |
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