CN101260330A - Front end combination purification technique for producing liquefied natural gas from mixture gas rich-containing methane - Google Patents
Front end combination purification technique for producing liquefied natural gas from mixture gas rich-containing methane Download PDFInfo
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- CN101260330A CN101260330A CNA2008100442707A CN200810044270A CN101260330A CN 101260330 A CN101260330 A CN 101260330A CN A2008100442707 A CNA2008100442707 A CN A2008100442707A CN 200810044270 A CN200810044270 A CN 200810044270A CN 101260330 A CN101260330 A CN 101260330A
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Abstract
The invention discloses a front-end combined purification process used to produce liquefied natural gas from mixed gas richly containing methane, which comprises four unit parts: acid gas removal, drying and dehydration, heavy hydrocarbon removal and demercuration. The mixed gas firstly undergoes a purification treatment through composite amine solution, CO2, H2S and HCN acid gases in the mixed gas are removed to the concentration less than or equal to 20ppm; the moisture in the gas is removed to a dew point at normal pressure less than or equal to minus 70 DEG C through isopiestic drying and dehydration treatment, then heavy hydrocarbon components above C5 are removed to the concentration less than or equal to 10ppm through temperature-changing pressure-changing absorption and purification treatment; finally the mercury content is removed to the value less than or equal to 0.001mu g/Nm<3> through the demercuration of demercuration adsorbent. The process has better purification effect than the conventional process route, improves the utilization rate of the raw materials and decreases the energy consumption during the purification; and the operation indexes of the units are easier to control.
Description
Technical field
The invention belongs to the front end purification treatment technology of methane-rich gas low-temperature liquefaction.Particularly, to from the mixed gas that is rich in methane, obtaining the industrialized unit of natural gas liquids (LNG), all need be before gas mixture carries out cryogenic liquefying with wherein contained acid gas components, water, high-carbon hydrocarbon are removed to the required precision of liquefaction, have only so, could guarantee that liquefying separation process and equipment can safe and stable operations.
Background technology
Under the pressure of environmental protection and energy cost pressure, Sweet natural gas promotes at social every field proportion just gradually as primary energy source, and its market demand also just increases sharply.The defeated method of supplying of traditional pipe still is a main flow, but limited by material condition and user distribution, there is quite a few resource can't carry out pipe long-distance and carries, need to select the mode of liquefaction, change methane into liquid and adopt again flexibly that mode of transport is sent to user terminal with it.
Methane component liquefaction is to obtain natural gas liquids (LNG) in the mixed gas of methane with being rich in, and its core technology is divided into two portions: the purification part of front end gas mixture and back level liquefaction part.According to the domestic a few cover LNG device running conditions that put into operation, its subject matter all is reflected in the gas mixture prime and purifies part.Be embodied in: 1. existing apparatus adopts the MEA solution process to remove sour gas (CO2, H2S, HCN) usually, because solution system instability, particularly in mixed gas, contain under the organosulfur situation, irreversible degraded easily takes place in solution, causes behind the amine system purification that acid gas components exceeds standard in the gas often; 2. existing apparatus all adopts the dehydration of single-stage alternating temperature pressure swing adsorption technique and takes off high-carbon hydrocarbon, there are two bigger shortcomings in this technology: one: with the process gas is resurgent gases, resurgent gases tolerance is very big, accounts for 25%～60% of technology body gas, has reduced the liquefied fraction of gas; Its two: moisture content and heavy hydrocarbon remove on same sorbent material, cause dry purification part load big, force system to reduce load operation, and a whole set of liquefying plant production capacity is descended.
Summary of the invention
The purpose of this invention is to provide a kind of front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids, make the present invention than the good purification of conventional operational path, improve raw material availability and reduce energy expenditure in the scavenging process, and each unit operation index is more prone to control.
The object of the present invention is achieved like this: a kind of front end combination purification technique of producing natural gas liquids from the mixed gas that is rich in methane comprises acid gas removal, drying and dehydrating, heavy hydrocarbon removes and four cell mesh of demercuration; Mixed gas is at first handled through the varies solution purification, with wherein CO2, H2S, HCN acid gas removal to≤20ppm, again in isobaric drying and dehydrating is handled gas moisture removal to dew points at normal pressure≤-70 ℃, handle through the alternating temperature pressure varying adsorption of purified then, the above heavy hydrocarbon component of C5 is removed to≤10ppm, after take off pump sorbent material demercuration and handle, mercury content is removed to≤0.001 μ g/Nm
3
Compared to existing technology, the invention has the beneficial effects as follows:
The present invention proposes a kind of brand-new purification process route.Adopt varies solution absorption isolation technique that acidic components in the methane rich gas mixture are removed to≤20ppm, this solution system has active high and very stable, degree of purification height, economical operation reliable characteristics; Adopt isobaric drying and dehydrating unit, the absorption of drying tower, heating and cooling process are almost operated under same pressure, and resurgent gases adopting process gas is after the regenerative process, return in the process gas.Compare traditional technology, liquefied gas yield improves 20% at least; Adopt two groups of above alternating temperature pressure swing adsorption techniques, the above heavy hydrocarbon component of C5 decreasing ratio height satisfies high methane gas liquefaction requirement fully.Simultaneously, the regeneration energy consumption can be reduced more than 40%, the liquefied methane productive rate can be improved more than 5%.
Useful technique effect of the present invention will further be set forth in conjunction with embodiment in further part.
Description of drawings
Fig. 1 is that the acid gas removal unit adopts one section to absorb/one section reclaiming process schema;
Fig. 2 is that the acid gas removal unit adopts two sections absorption/two-stage regeneration process flow sheets;
Fig. 3 is the unitary process flow sheet of drying and dehydrating;
Fig. 4 is that heavy hydrocarbon removes the process flow sheet that the unit adopts two sections adsorption towers;
Fig. 5 is that heavy hydrocarbon removes the process flow sheet that the unit adopts three sections adsorption towers;
Fig. 6 is the process flow sheet of one embodiment of the invention.
Embodiment
The present invention comprises acid gas removal, drying and dehydrating, heavy hydrocarbon removes and four cell mesh of demercuration; Mixed gas is at first handled through the varies solution purification, with wherein CO2, H2S, HCN acid gas removal to≤20ppm, again in isobaric drying and dehydrating is handled gas moisture removal to dew points at normal pressure≤-70 ℃, handle through the alternating temperature pressure varying adsorption of purified then, the above heavy hydrocarbon component of C5 is removed to≤10ppm, after take off pump sorbent material demercuration and handle, mercury content is removed to≤0.001 μ g/Nm
3
1.0 sour gas remove the unit
The removing of sour gas in the high methane gas can adopt one section to absorb/one section reclaiming process, also can adopt two sections absorption/two-stage regeneration technologies.The acid gas removal unit can adopt one section to absorb/one section regeneration or two sections absorption/two-stage regeneration technologies according to mixture pressure and acid gas components content; Described varies solution content consists of: AMP3%～6%, and monoethanolamine 1%～5%, all the other are methyldiethanolamine.
Activator-1:AMP (2-amino-2-methyl-1-propanol), molecular weight: 89.1, molecular formula: (CH3) 2CCH2 (OH) NH2, consumption: 3%～6%,
Activator-2: monoethanolamine, molecular weight: 61, molecular formula: OHCH
2CH
2NH
2, consumption 1%～5%.
One section absorbs/one section reclaiming process and is described as follows:
Referring to accompanying drawing 1
In the acid gas removal unit, mixture pressure should be at 1.0MPa.G～15.0MPa.G (gauge pressure), its content of acid gas at 0.01%～50%.W (weight percent);
1 bottom enters the methane rich gas mixture from the absorption tower, fully contact with the varies solution that comes from top to bottom is reverse by the absorption tower packing layer from bottom to top, sour gas in the methane-riched gas mixture (CO2+H2S+HCN) is absorbed and enters liquid phase, unabsorbed component leaves the absorption tower in 1 top from the absorption tower, be cooled to normal temperature through water cooler 2, enter air water separator 3 then gas-liquid separation.Leave the sour gas (CO in the gas of air water separator 3
2+ H
2S+HCN) total amount is removed to≤20ppm, is sent to moisture removal of the present invention unit.
The solvent of acid gas absorption adopts varies solution, and absorption agent uses at acid gas removal unit internal recycle, and its circulation route is:
In absorption tower 1, absorbed the varies solution (title rich solution) of sour gas, after leaving the absorption tower from 1 bottom, absorption tower, in poor rich liquid heat exchanger 6, carry out heat exchange with the effusive solution in regenerator column 7 bottoms (lean solution), rich solution is warmed up to～98 ℃ of tops of removing regenerator column 7, carry out steam stripping regeneration at regenerator column 7, the sour gas that is absorbed in the solution is parsed, after the poor degree of lean solution touches the mark, leave regenerator column 7 from the regenerator column bottom.The lean solution that goes out regenerator column 7 is passed through poor rich liquid heat exchanger 6, lean solution water cooler 5, lean pump 4 successively, and 1 top enters the absorption tower from the absorption tower after metering.
From the sour gas of regenerator column 7 top exits, through water cooler 9, air water separator 10, the sour gas that contains methane of normal temperature is sent and is out-of-bounds made his usefulness.Phlegma returns sloptank 13.(having among Fig. 1: solution strainer 8, solution storage tank 12).
The sour gas required heat of regenerating from absorption agent is provided by the reboiler 11 of regenerator column 7 bottoms, and the required thermal source of regenerating can be steam or other thermal barrier (as thermal oil, high-temperature gas or liquid).
Adopt two sections absorption/two-stage regeneration technologies, its process description is as follows:
Referring to accompanying drawing 2
The methane rich gas mixture enters from 1a bottom, absorption tower, passes through the absorption tower from bottom to top; Varies solution (lean solution) after the holomorphosis enters from 1a top, absorption tower, passes through the absorption tower from top to bottom; The varies solution (semi lean solution) of incomplete regen-eration enters from absorption tower 1a middle part, passes through the absorption tower from top to bottom; The varies solution of countercurrent flow fully contacts in the absorption tower with gas mixture, sour gas in the gas mixture is absorbed and enters liquid phase, unabsorbed component is drawn from absorbing cat head 1a portion, earlier through water cooler 2a be cooled to≤40 ℃, enter purified gas then and divide flow container 3a to separate the gas-liquid component, the gas that the goes out minute flow container branch that anhydrates removes the unit.
The solvent of acid gas absorption adopts varies solution, and absorption agent uses at acid gas removal unit internal recycle, and its circulation route is:
Varies solution behind the absorption sour gas claims rich solution, the rich solution that leaves absorption tower 1a goes earlier the bottom vacuum flashing of regenerator column 9a, the part sour gas desorbs from solution, solution enters the top of regenerator column 9a again, by steam and sour gas stripping, obtain the solution (being called semi lean solution) of partial regeneration on regenerator column top.
Semi lean solution is about 30%～80% of solution circulated total amount, delivers to the middle part, absorption tower by semi-leanpump 17a.Remaining semi lean solution is extracted out by solution pump 4a, and after interchanger 8a was by the lean solution temperature raising, hot reactivation was carried out on the top that enters the hypomere (stripping stage) of regenerator column 9a again.The regenerated thermal source provides (heating agent is thermal oil or low-pressure saturated steam) by reboiler 10a.
From the lean solution that regenerator column 9a comes out, through interchanger 8a heat exchange, lean pump 6a pressurization after water cooler 7a cooling, enters the absorption tower from 1a top, absorption tower again.
Varies solution removes the sour gas in the high methane gas, and being rich in methane blended gas working pressure scope can select by any one pressure spot in 1.0Mpa.G～15.0Mpa.G.
Varies solution removes the sour gas in the high methane gas, and wherein acid gas components content is in 0.01%～60%.
Determine to adopt one section according to flow, acid gas components content and the dividing potential drop of unstripped gas and absorb/one section regeneration or two sections absorption/two-stage regeneration technologies.
2.0 drying and dehydrating unit
Referring to accompanying drawing 3
The moisture removal unit is made up of three moisture eliminators, a well heater, a water cooler, a separator.Two is main moisture eliminator in three moisture eliminators, and one is the drying aid device.Main moisture eliminator drying and regeneration hocket, and regeneration divides heating and cooling two steps, and product gas dew points at normal pressure after drying is lower than-75 ℃.
The moisture removal unit adopts isobaric TSA drying process, the absorption, the heating and cooling process that are drying tower are operated under almost same pressure, resurgent gases adopting process gas, after regenerative process is finished, return in the process gas, therefore, regenerative process does not need other resurgent gases, this technology is compared with traditional technology, can improve LNG productive rate 20% at least.
Be example now, this unitary operating process be described with an adsorption tower 1:
The gas that comes from the acid gas removal unit, at first be divided into two-way through flow control valve: the one tunnel as resurgent gases, and one the tunnel as mainstream gas.Wherein mainstream gas is directly removed drying tower 1b through valve V1, and the siccative that loads among the drying tower 1b gets off the water adsorption in the gas gas, makes gas be able to drying, and gas obtains qualified gas through valve V2, goes heavy hydrocarbon to remove the unit.
Another drying tower 2b is in regenerative process:
The regenerative process of drying tower 2b comprises thermal regeneration and two steps of blast-cold.
In the thermal regeneration process, resurgent gases is successively through valve V11, drying tower 3b, well heater 4b, valve V8, drying tower 2b, valve V6, valve V10, water cooler 6b, water separator 5b, converge with process gas again, enter the drying tower 1b that is in adsorbed state through valve V1, finish heat-processed drying tower 2b.
From the route of gas process as can be seen:
1), resurgent gases returns mainstream gas, do not need external any carrier gas in the thermal regeneration process.
2), when drying tower 2b is heated, regeneration gas cools off drying tower 3b, drying tower 3b internal adsorption agent and material accumulation of heat is taken away entered well heater 4b again, reduces the required energy expenditure of thermal regeneration.
3), resurgent gases entering before the drying tower 2b, super-dry tower 3b is predrying, the moisture content in the resurgent gases seldom, and is fine to the drying effect of drying tower 2b.
In process of cooling, resurgent gases is successively through valve V9, valve V6, drying tower 2b, valve V8, well heater 4b, drying tower 3b, V12, water cooler 6b, water separator 5b, converge with process gas again, enter the drying tower 1b that is in adsorbed state through valve V1, finish process of cooling drying tower 2b.Process of cooling exists too:
1), resurgent gases returns mainstream gas, do not need external any carrier gas in the thermal regeneration process.
2), drying tower 2b is being carried out refrigerative simultaneously, regeneration gas heats drying tower 3b, drying tower 2b internal adsorption agent and material accumulation of heat is taken away entered well heater 4b again, reduces the required energy expenditure of thermal regeneration.
3), resurgent gases entering before the drying tower 3b, super-dry tower 2b is predrying, the moisture content in the resurgent gases seldom, and is fine to the drying effect of drying tower 3b.
Drying tower 2b waits for entering absorption next time through after the above-mentioned heating and cooling process.
The regenerative process of the regenerative process of drying tower 1b and drying tower 2b is just the same, just needs the numbering difference of action valve.
Two drying towers are taken turns flow operations, can reach the ability of continuous processing gas.
Siccative is selected according to the requirement of dehydration precision, can adopt the porous mass stronger to the water adsorptive power, as the combination of one or more sorbent materials in activated alumina, silica gel, the molecular sieve.For methane-rich gas is the drying of the purpose of LNG, and molecular sieve is indispensable sorbent material.
The regeneration Heating temperature is determined according to the combination of dehydration accuracy requirement and sorbent material, is the drying of the purpose of LNG for methane-rich gas, and regeneration temperature is generally between 180～320 ℃.
3.0 heavy hydrocarbon removes the unit
After the methane rich gas mixture removes sour gas and water, remove high-carbon hydrocarbon through alternating temperature transformation absorption (PTSA).Device is provided with two or many adsorbers.Wherein one absorption and other adsorber is in regeneration step.
The operating process explanation of two tower process:
Referring to accompanying drawing 4
Be how example explanation technological process realizes now with adsorber 1:
A, adsorption process: remove the process gas behind sour gas and the moisture, enter the adsorption tower 1c that is in adsorbed state from adsorption tower 1c bottom through valve V1A.Under the selection of sorbent material absorption, high-carbon hydrocarbon component wherein is adsorbed, and the gas that is not adsorbed flows out through valve V2A from cat head, obtains qualified Purge gas and goes back operation (LNG liquefy operation).When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off unstripped gas feed valve V1A and the product gas outlet valve V2A of this adsorption tower 1c, stop absorption.Adsorption bed begins to change over to regenerative process.
B, the contrary journey of letting slip: this is after adsorption process finishes, and opens valve V5A and reduces pressure against the absorption direction, the process that the gas decompression that is adsorbed is desorbed.Decompression process enters the low-pressure fuel gas pipe network reposefully by pressure regulator valve.
C, heat-processed: this is to let slip after journey finishes contrary, adopts noncondensable gas (BOG) after the mixed gas liquefaction as carrier gas, and BOG is through valve V7, well heater 3c, valve V4A, V5A, water cooler 4c, valve V9.Carrier gas flushing after the heating is adsorbent bed, and the impurity that is adsorbed on the sorbent material is desorbed fully, makes sorbent material obtain regenerated process (among Fig. 4, interchanger 4c).
D, blast-cold process: after heat-processed is finished, open the by-pass valve V8 of well heater, utilize cold BOG gas that adsorption tower is carried out blast-cold from top to bottom, this end of processing when temperature out arrives normal temperature.
E, the process of boosting: after the blast-cold process is finished, the process of using the pure gas from another adsorption tower 2c that this adsorption tower is boosted.In order adsorption tower can be switched to reposefully adsorb and to guarantee that product purity does not fluctuate in this course next time, need slowly and reposefully adsorption column pressure be risen to adsorptive pressure by the variable valve that boosts with purified gas, with guarantee product boost process fully and reduce influence to the adsorptive pressure fluctuation.
When system be in contrary put and when all pressing BOG gas directly remove the low-pressure fuel gas pipe network.
Adsorption tower has just been finished complete " adsorption-regeneration " circulation after this process, gets ready for absorption next time again.Two adsorption tower wheel flow operations reach continuous processing gas.
The operating process explanation of three tower process:
Referring to accompanying drawing 5
Be how example explanation technological process realizes now with adsorber 1d:
A, adsorption process: remove the process gas behind sour gas and the moisture, enter the adsorption tower 1d that is in adsorbed state from adsorption tower 1d bottom through valve V1A.Under the selection of sorbent material absorption, high-carbon hydrocarbon component wherein is adsorbed, and the gas that is not adsorbed flows out through valve V2A from cat head, obtains qualified Purge gas and goes back operation (LNG liquefy operation).When the mass transfer zone forward position (being called absorb leading-edge) that is adsorbed impurity arrives bed outlet reservation section, turn off unstripped gas feed valve V1A and the product gas outlet valve V2A of this adsorption tower 1d, stop absorption.Adsorption bed begins to change over to regenerative process.
B, the contrary journey of letting slip: this is after adsorption process finishes, and opens valve V6A and reduces pressure against the absorption direction, the process that the gas decompression that is adsorbed is desorbed.Decompression process enters the low-pressure fuel gas pipe network reposefully by pressure regulator valve.This moment, adsorption tower 2d was in adsorbed state.
C, heat-processed: this is to let slip after journey finishes contrary, adopts noncondensable gas (BOG) after the mixed gas liquefaction as carrier gas, and BOG is through valve V4C, adsorption tower 3d, valve V7C, well heater 4d, valve V5A, adsorption tower 1, valve V6A, water cooler 5d, valve V8.Carrier gas flushing after the heating is adsorbent bed, and the impurity that is adsorbed on the sorbent material is desorbed fully, makes sorbent material obtain the regenerated process.This moment, adsorption tower 3d was in the blast-cold process.
D, blast-cold process: after heat-processed is finished, change the blast-cold process over to, resurgent gases is passed through successively: valve V4A, adsorption tower 1d, valve V7A, well heater 4d, valve V5B, adsorption tower 2d, valve V6B, water cooler 5d, valve V8, adsorption tower 1d is carried out blast-cold from top to bottom, this end of processing when temperature out arrives normal temperature.This moment, adsorption tower 3d was in adsorbed state.
E, the process of boosting: after the blast-cold process is finished, use from the pure gas of another adsorption tower the process that this adsorption tower is boosted through valve V7, valve V3.In order adsorption tower can be switched to reposefully adsorb and to guarantee that product purity does not fluctuate in this course next time, need slowly and reposefully adsorption column pressure be risen to adsorptive pressure by the variable valve that boosts with purified gas, with guarantee product boost process fully and reduce influence to the adsorptive pressure fluctuation.
When system be in contrary put and when all pressing BOG gas directly remove the low-pressure fuel gas pipe network.
Adsorption tower has just been finished complete " adsorption-regeneration " circulation after this process, gets ready for absorption next time again.Three adsorption towers are taken turns flow operations, reach the purpose of continuous purification gas.
So far, after above-mentioned acid gas removal, moisture removal, heavy hydrocarbon removed, its decontamination index was as follows for methane-riched gas mixture (comprising natural gas, coal tail gas, biogas, coke(oven)gas, coal gas etc.):
(CO
2+H
2S+HCN) ≤20ppm
Dew point (normal pressure)≤-70 ℃
High-carbon hydrocarbon (the above component of C5)≤10ppm
Purge gas has satisfied methane-rich gas liquefaction requirement.
The demercuration unit adopts the two bed type flow process, and two can parallel connection or series operation; The filling demercuration adsorbent is a sulfur loading active carbon in the bed.
Pipe natural gas is produced natural gas liquids (LNG)
1, material condition
Form
Flow: 10000Nm3/h
Pressure: 2.5Mpa.G～3.5Mpa.G
2, purify requirement
Water-content≤1ppm
Benzene content≤10ppm
CO2 ≤20ppm
∑S ≤1ppm
Dew points at normal pressure≤-70 ℃
3, process description
Fig. 6 illustrates, Sweet natural gas is by out-of-bounds introducing, at first enter the varies absorption system. because content of acid gas is low in the unstripped gas, the solution circulated amount is little, adopt two sections absorption/two-stage regeneration flow processs, energy-conservation limited, make flow process complicated on the contrary. thereby adopt one section to absorb/one section regeneration flow process. CO2≤20ppm in the Sweet natural gas after the varies absorption system purifies, advance isobaric regeneration dewatering unit. go out in this unit Sweet natural gas water-content dew points at normal pressure≤-70 ℃. enter the alternating temperature psa unit again, relate to the meter material condition at this programme, adopt three-tower type PTSA technology. tower absorption, two towers are in regeneration step in addition. Sweet natural gas medium high carbon hydrocarbon (benzene) content≤10ppm after the absorption of alternating temperature transformation.Simultaneously, can reduce the regeneration energy consumption more than 40%, regeneration is the noncondensable gas (BOG) that adopts liquefaction system to discharge, and can improve the liquefied methane productive rate more than 5%.
1.0 material condition
Form
| Component | CO2 | CH4 | H2S | ∑ |
| Form (%V) | 44.5 | 54 | 1.5 | 100.00 |
Flow: 7000Nm3/h
Pressure: 2.0Mpa.G
2.0 purification requirement
Water-content≤1ppm
Benzene content≤10ppm
CO2 ≤20ppm
∑S ≤1ppm
Dew points at normal pressure≤-70 ℃
3, process description
Sweet natural gas at first enters the varies absorption system by out-of-bounds introducing. because content of acid gas height in the unstripped gas, the solution circulated amount is big, adopts two sections absorption/two-stage regeneration flow processs, and energy-saving effect is obvious, so the acid gas removal unit is two sections flow processs.(CO2+H2S)≤20ppm in the Sweet natural gas after the varies absorption system purifies, advance isobaric regeneration dewatering unit. go out in this unit Sweet natural gas water-content dew points at normal pressure≤-70 ℃. enter the alternating temperature psa unit again, relate to the meter material condition at this programme, adopt three-tower type PTSA technology. tower absorption, two towers are in regeneration step in addition. Sweet natural gas medium high carbon hydrocarbon (benzene) content≤10ppm after the absorption of alternating temperature transformation.
Claims (9)
1, a kind of front end combination purification technique of producing natural gas liquids from the mixed gas that is rich in methane is characterized in that: comprise acid gas removal, drying and dehydrating, heavy hydrocarbon removes and four cell mesh of demercuration; Mixed gas is at first handled through the varies solution purification, with wherein CO2, H2S, HCN acid gas removal to≤20ppm, again in isobaric drying and dehydrating is handled gas moisture removal to dew points at normal pressure≤-70 ℃, handle through the alternating temperature pressure varying adsorption of purified then, the above heavy hydrocarbon component of C5 is removed to≤10ppm, after take off pump sorbent material demercuration and handle, mercury content is removed to≤0.001 μ g/Nm
3
2, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 1, it is characterized in that: described acid gas removal unit can adopt one section to absorb/one section regeneration or two sections absorption/two-stage regeneration technologies according to mixture pressure and acid gas components content; Described varies solution content consists of: AMP 3%～6%, monoethanolamine 1%～5%, and all the other are methyldiethanolamine.
3, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 2, it is characterized in that: in the described acid gas removal unit, mixture pressure should be at 1.0MPa.G～15.0MPa.G, its content of acid gas at 0.01%～50%.W; One section absorbs in/one section reclaiming process, gas mixture is removed mechanical drop through separating gas earlier, again from the absorption tower from bottom to top with from top to bottom, the varies solution of countercurrent flow fully contacts in the absorption tower, sour gas in the gas is absorbed and enters liquid phase, unabsorbed component is drawn from the adsorption tower top, earlier through water cooler be cooled to≤40 ℃, enter purified gas then and divide flow container, go out that sour gas is removed to≤20ppm in the gas of minute flow container, be sent to the drying and dehydrating unit, phlegma removes sloptank; The effusive varies rich solution from the absorption tower after the effusive lean solution heat exchange in regenerator column bottom, is warmed up to 98 ℃ and goes to regenerator column top, carries out steam stripping regeneration at regenerator column, touches the mark until the poor degree of lean solution.
4, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 2, it is characterized in that: described two sections absorb in/two sections reclaiming procesies, the methane rich gas mixture enters from the bottom, absorption tower, passes through the absorption tower from bottom to top; Varies solution (lean solution) after the holomorphosis enters from top, absorption tower, passes through the absorption tower from top to bottom; The varies solution (semi lean solution) of incomplete regen-eration enters from the middle part, absorption tower, passes through the absorption tower from top to bottom; The varies solution of countercurrent flow fully contacts in the absorption tower with gas mixture, sour gas in the gas mixture is absorbed and enters liquid phase, unabsorbed component is drawn from the top, absorption tower, earlier through water cooler be cooled to≤40 ℃, enter purified gas then and divide flow container to separate the gas-liquid component, the gas that the goes out minute flow container branch that anhydrates removes the unit; Varies solution behind the absorption sour gas claims rich solution, the rich solution that leaves the absorption tower goes earlier the bottom vacuum flashing of regenerator column, the part sour gas desorbs from solution, solution enters the top of regenerator column again, by steam and sour gas stripping, obtain the semi lean solution of partial regeneration on regenerator column top; Semi lean solution is about 30%～80% of solution circulated total amount, delivers to the middle part, absorption tower by semi-leanpump.Remaining semi lean solution is extracted out by solution pump, and after interchanger was by the lean solution temperature raising, hot reactivation was carried out on the top that enters the bottom stripping stage of regenerator column again; Lean solution from regenerator column comes out after the heat exchange cooling, enters the absorption tower from top, absorption tower.
5, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 1, it is characterized in that: described drying and dehydrating unit adopts isobaric drying process, with the technology methane-rich gas as regeneration gas, after the water sepn that removes out, in this part resurgent gases retrieval system process gas.
6, according to the described front end combination purification technique of producing natural gas liquids from the mixed gas that is rich in methane of claim 5, it is characterized in that: described drying and dehydrating system is made up of three moisture eliminators, a well heater, a water cooler, a separator; Two is main moisture eliminator in three moisture eliminators, and one is the drying aid device.Main moisture eliminator drying and regeneration hocket, and regeneration divides heating and cooling two steps, and product gas dew points at normal pressure after drying is lower than-70 ℃; Described gas to be dried at first is divided into two-way through flow control valve: wherein one the tunnel directly remove drying tower, wherein Zhuan Tian siccative gets off the water adsorption in the gas gas, makes gas be able to drying; Be under the dry status at a drying tower, another drying tower is in regenerative process; The regenerative process of drying tower comprises thermal regeneration and two steps of blast-cold, in the thermal regeneration process, another road gas at first carries out drying through predrying tower, then heater via be warming up to～200 ℃ of post-flush need the regenerated drying tower, sorbent material intensification, moisture are wherein desorbed, stripping gas mixes with another road gas behind cooling and separatory again, and drying is carried out in the drying tower of drying regime in the place to go then; In the blast-cold process, the direct place to go of regeneration gas is in the drying tower of reproduced state, the drying tower temperature is reduced to normal temperature, and then remove predrying tower after the heater via heating, siccative in the predrying tower is carried out heat drying, mix with another road gas behind cooling and separatory then, drying is carried out in the drying tower of drying regime in last place to go again.
7, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 1, it is characterized in that: described heavy hydrocarbon removes the unit and adopts purification adsorption tower alternating temperature pressure swing adsorption technique more than two or two, and the above heavy hydrocarbon of C5 in the high methane gas is removed to≤10ppm.
8, according to the described front end combination purification technique of from the mixed gas that is rich in methane, producing natural gas liquids of claim 7, it is characterized in that: described heavy hydrocarbon removes in the unit, two or the experience absorption successively in a loop cycle of two above adsorption towers, contraryly put, heating, blast-cold, processing step boosts, wherein a purification adsorber is in the absorbing process step, and other purifies adsorber and is in regeneration step.
9, according to the described front end combination purification technique of producing natural gas liquids from the mixed gas that is rich in methane of claim 1, it is characterized in that: described demercuration unit adopts the two bed type flow process, and two can parallel connection or series operation; The filling demercuration adsorbent is a sulfur loading active carbon in the bed.
Priority Applications (1)
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