CN202595073U - Natural gas drying and liquefying device - Google Patents
Natural gas drying and liquefying device Download PDFInfo
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- CN202595073U CN202595073U CN 201220186602 CN201220186602U CN202595073U CN 202595073 U CN202595073 U CN 202595073U CN 201220186602 CN201220186602 CN 201220186602 CN 201220186602 U CN201220186602 U CN 201220186602U CN 202595073 U CN202595073 U CN 202595073U
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Abstract
The utility model relates to a natural gas drying and liquefying device. The natural gas drying and liquefying device comprises an adsorption drying system, a refrigerant compression system and a cold box system, wherein the cold box system comprises a group of plate-fin heat exchanger assembly, a natural gas water separating tank, a heavy hydrocarbon separator and two throttling devices. According to the natural gas drying and liquefying device disclosed by the utility model, improvement is carried out on the basis of the traditional technology device, virgin gas is firstly fed to a cold box for pre-cooling, condensed water can be then separated from the virgin gas after the virgin gas enters into the natural gas water separating tank, more than 70 wt% of water in the virgin gas can be removed, the virgin gas can be then fed to the adsorption drying system for deep dewatering, the load of the natural gas drying system can be obviously reduced, the size of a drying device can be reduced, and the consumption of an adsorbing agent can be reduced.
Description
Technical field
The utility model relates to the purification and the liquefaction of being rich in hydrocarbon gas to be produced, and is specifically related to a kind of Sweet natural gas drying and liquefying plant.
Background technology
Sweet natural gas is owing to its feature of environmental protection becomes the optimisation substance that replaces other fuel, and its Application Areas expands aspects such as generating, automobile usefulness gas, industrial gas, city resident's usefulness gas, chemical industry usefulness gas gradually to.Along with the growth of natural gas consumption amount, the most effectively supply with one of form as Sweet natural gas, the volume of trade of natural gas liquids has also become one of fastest-rising field of energy market.The continuous development of natural gas liquids industry is then had higher requirement at aspects such as energy consumption, investment and efficient to natural gas liquefaction and device and natural gas conditioning method and apparatus in earlier stage.
At present, in the natural gas conditioning and liquefaction process of comparative maturity, adopting more is process method as shown in Figure 1.For guaranteeing liquefaction process and device security steady running, before virgin gas carries out cryogenic liquefying, needing wherein, contained acid gas components, water etc. are removed to the required precision of liquefaction.As shown in fig. 1, virgin gas at first gets into the depickling system, removes sour gas such as CO therein
2, H
2S etc., after content of acid gas was qualified, the mixed gas that goes out the depickling system and contain saturation water directly went dewatering system to carry out deep dehydration, and the dry natural gas that reaches after the required precision goes the liquefaction of ice chest system.
In the above-mentioned traditional technology, advance in the Sweet natural gas of dewatering system because carried saturation water when going out the depickling system, when the virgin gas treatment capacity is big such as direct entering dewatering system can cause bigger load to dewatering system.To this problem, the utility model has been done corresponding improvement, before mixed gas gets into dewatering system, dewaters in advance, thereby significantly reduces the dewatering system load, reduces the size of dehydration equipment and reduces the dehydrated adsorbent consumption.
The utility model content
The utility model adopts the dry and natural gas liquids of a kind of brand-new technical process.
The utility model provides a kind of Sweet natural gas drying and liquefying plant, and its device comprises absorption drying system, refrigerant compression systems and ice chest system.Vapor phase refrigerant that this refrigerant compression systems produces and liquid phase refrigerant return cryogen compression system inlet through the cryogen backward channel for the ice chest system after cold is provided; The ice chest system comprises one group of plate-fin heat exchanger group, two throttling sets that are connected with the heat exchanger channels of said plate-fin heat exchanger group, a Sweet natural gas water distributing can that is connected with a heat exchanger channels of said plate-fin heat exchanger group and a Sweet natural gas heavy hydrocarbon separator that is connected with another heat exchanger channels of said plate-fin heat exchanger group.The utility model institute adopting process flow process is at first sent Sweet natural gas to be dried into precooling in the ice chest; It is above (more than the preferred 80wt% to slough wherein 70wt%; More preferably more than the 85wt%; More than the preferred especially 90wt%) moisture, thereby significantly reduce the load of Sweet natural gas dehumidification system, reduce the drying plant size and reduce the sorbent material consumption.
Embodiment as the utility model; Sweet natural gas after the depickling (virgin gas) pipeline connects Sweet natural gas water distributing can middle part through heat exchanger package one gas phase channel; The top gas phase channel of Sweet natural gas water distributing can connects the inlet of absorption drying system; Connect the heavy hydrocarbon separator behind another gas phase channel of the outlet conduit connection heat exchanger package of absorption drying system, heavy hydrocarbon separator top gas phase end is through pass through heat exchanger package subsequent stages interchanger successively behind the next gas phase channel of heat exchanger package;
The cold of ice chest system is provided by the refrigeration agent that refrigerant compression systems produces; Liquid phase refrigerant pipeline by refrigerant compression systems is through an end of the liquid channel connection first throttle device of heat exchanger package, and the other end of first throttle device is connected with the cryogen backward channel of interchanger; The vapor phase refrigerant pipeline that is come by the cryogen compression system connects an end of second throttling set through the cryogen gas phase channel of heat exchanger package, and the other end of second throttling set connects the inlet that connects refrigerant compression systems behind the cryogen backward channel.
The technical scheme of the utility model is summarized as follows:
A kind of Sweet natural gas drying and liquefying plant, this device comprise absorption drying system, refrigerant compression systems and ice chest system,
Wherein refrigerant compression systems has: gas phase cryogen exit passageway, liquid phase cryogen exit passageway and access road;
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth; Said first heat exchanger channels is connected with gas phase cryogen exit passageway with the liquid phase cryogen exit passageway of said refrigerant compression systems respectively via two pipelines with second heat exchanger channels, and the 3rd heat exchanger channels is connected with the access road of said refrigerant compression systems;
First throttling set that is connected with the 3rd heat exchanger channels with first heat exchanger channels of said plate-fin heat exchanger group;
Second throttling set that is connected with the 3rd heat exchanger channels with second heat exchanger channels of said plate-fin heat exchanger group; With
With a heat exchanger channels of said plate-fin heat exchanger group is the Sweet natural gas water distributing can that the 4th heat exchanger channels is connected,
Inlet end is the Sweet natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected with another heat exchanger channels of said plate-fin heat exchanger group;
Be used to carry that Sweet natural gas (is a virgin gas after the depickling; Or be called " remove sour gas after Sweet natural gas ") above-mentioned four heat exchanger channels of pipeline through heat exchanger package be connected to the Sweet natural gas water distributing can; Sweet natural gas water distributing can top gas phase end connects an access road of absorption drying system; An exit passageway of absorption drying system connects the inlet of the 5th heat exchanger channels of plate-fin heat exchanger group in the ice chest; The outlet of the 5th heat exchanger channels is connected to the heavy hydrocarbon separator, and the heat exchanger channels that the top gas phase end of heavy hydrocarbon separator passes through heat exchanger package is a cooling box behind the 6th heat exchanger channels.
Optional is, the top gas phase end of heavy hydrocarbon separator successively through behind the 6th heat exchanger channels of heat exchanger package further through cooling box behind other the 7th heat exchanger channels of heat exchanger package.
In this application, pressure unit MPaA is a MPa, absolute pressure." choosing " expression in this application wantonly is with or without." adsorption dry " and " dry absorption " interchangeable use in this application." drying tower " and " adsorption tower " interchangeable use.
Absorption drying system can adopt this area absorption drying system commonly used, preferably adopts the isobaric adsorption dry flow process of two towers or three towers, adopts molecular sieve adsorbing and dewatering, can be with moisture removal to dew points at normal pressure≤-76 ℃.
According to preferred embodiment, wherein absorption drying system comprises:
First drying tower (T1) and second drying tower (T2), the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (T3),
Well heater (E1),
Gas-liquid separator (T4) and
Water cooler (E2),
Each drying tower has one or two or a plurality of sorbent material composite bed,
The transfer of gas pipe that is rich in methane after the depickling is divided into two branch roads i.e. first branch road and second branch road, and first valve (V1) wherein is set on first branch road; Divide three the tunnel to lead to liquefaction system via ingress pipe, the first drying tower T1 and the 3rd valve (V3) of second valve (V2), first drying tower (T1) respectively afterwards again at first valve (V1); Ingress pipe, second drying tower (T2) and the 5th valve (V5) via the 4th valve (V4), second drying tower (T2) lead to liquefaction system, and are connected to the derivation port of water cooler (E2) via the ingress pipe of the delivery line of optional valve, gas-liquid separator (T4), gas-liquid separator (T4), gas-liquid separator (T4); Above-mentioned second branch road is connected to the ingress pipe of water cooler (E2) respectively via the tenth valve (V10) and the 11 valve (V11) with via the 12 valve (V12) and the 13 valve (V13); Draw arm between first drying tower (T1) and the 3rd valve (V3) and between second drying tower (T2) and the 5th valve (V5), drawing arm; These two arms converge an end that is connected to well heater (E1) via the 8th valve (V8) and the 9th valve (V9) respectively afterwards; The other end of well heater is connected to an end of the 3rd drying tower (T3), the other end of drying tower (T3) via pipe connection on the pipeline between the 12 valve (V12) and the 13 valve (V13); Drawing arm between first drying tower (T1) and second valve (V2) and between second drying tower (T2) and the 4th valve (V4), drawing arm, these two arms converge afterwards via the 6th valve (V6) and the 7th valve (V7) respectively and are connected on the pipeline between the tenth valve (V10) and the 11 valve (V11).
Generally, control the carrying out of each process by means of each valve.
More preferably, each drying tower has at least one independently, and 32 at the most, preferred 2-16, more preferably 4-16, further preferred 6-14, further preferred 8-12 adsorbent bed or composite bed still.Each sorbent material composite bed of each drying tower loads one or both or the multiple sorbent material that is selected from 3A or 4A molecular sieve, activated alumina, gac and the water-fast silica gel independently; Wherein 3A molecular sieve, 4A molecular sieve or activated alumina are as dehydrated adsorbent, and gac or water-fast silica gel are as taking off the heavy hydrocarbon sorbent material.Further preferably, each adsorption tower has at least one the molecular sieve adsorbent bed layer and optional at least one acticarbon bed that is used to take off heavy hydrocarbon that is used to dewater; Preferred each adsorption tower has 2-16, preferred 3-12, more preferably 3-8 of being used to dewater, more preferably 2-16, preferred 3-12 of heavy hydrocarbon, more preferably individual, more preferably 4-6 acticarbon bed of 3-8 are taken off in 4-6 molecular sieve adsorbent bed layer and optional being used to.
Operating process is described below.
Described a kind of Sweet natural gas drying of the utility model and liquid device; Its virgin gas at first the 4th heat exchanger channels of process heat exchanger package gets into the Sweet natural gas water distributing can after being cooled to certain temperature; Isolate the moisture that condensation is got off from pot bottom; Sweet natural gas water distributing can top gas phase partly gets into and adopts isobaric adsorption dry technology deep dehydration in the absorption drying system, after the 6th heat exchanger channels of dried Sweet natural gas entering heat exchanger package is cooled to certain temperature, gets in the heavy hydrocarbon separator and separates; The bottom obtains the heavy hydrocarbon component; The gas phase part that the top obtains is carried out heat exchange through all the other interchanger at different levels that the 6th heat exchanger channels continues the entering heat exchanger package, is cooled to supercooled state, exports the natural gas liquids (LNG) that obtains from ice chest.
The cold of ice chest system is provided by the refrigeration agent from the refrigeration agent compression system; First heat exchanger channels that the liquid cryogen that is come by refrigerant compression systems gets into heat exchanger package by precooling after again through the first throttle device, this stream after the throttling strand is back in the 3rd heat exchanger channels of heat exchanger package cold is provided; The gas phase cryogen that is come by refrigerant compression systems carries out throttling via second heat exchanger channels of heat exchanger package, second throttling set of flowing through again after by precooling, in the 3rd heat exchanger channels of burst reverse entering heat exchanger package of this stream after the throttling cold is provided.Be transferred the inlet of getting back to refrigerant compression systems from the effusive azeotrope of the 3rd heat exchanger channels.
A kind of Sweet natural gas drying and the technical process that liquefying plant adopted are following:
The plate-fin heat exchanger group that the raw natural gas of (after promptly removing sour gas) at first gets in the ice chest after the depickling is carried out precooling; Go out heat exchanger package after being cooled to 5 ℃～20 ℃; Get into the Sweet natural gas water distributing can and slough moisture from pot bottom; Sweet natural gas water distributing can top gas phase continues to get into the absorption drying system dehydration, after the Sweet natural gas after the dehydration returns and is cooled to-30 ℃～-60 ℃ in the follow-up interchanger of heat exchanger package, goes out the plate-fin heat exchanger group and gets into the heavy hydrocarbon separator and carry out gas-liquid separation; Heavy hydrocarbon separator bottom obtains heavy hydrocarbon; Continue to get into all the other interchanger at different levels of heat exchanger package by the isolated vapor phase stream thigh in heavy hydrocarbon separator top, and cooling box after being cooled to-130 ℃～-166 ℃ therein, natural gas liquids (LNG) obtained.
Refrigeration agent circulation technology flow process:
The liquid phase refrigerant that comes from refrigerant compression systems at first gets into first heat exchanger channels of heat exchanger package; Therein by-30 ℃～-80 ℃ extremely approximately of precoolings; Behind throttling valve throttling to 0.2～0.8MPaA, get into cryogen backward channel (i.e. the 3rd heat exchanger channels); Strand converge with the refrigeration agent that returns from the follow-up interchanger of heat exchanger package stream, for heat exchanger package provides cooling box behind the cold; By refrigerant compression systems come second heat exchanger channels of gas phase refrigeration through heat exchanger package be cooled to-135 ℃～-169 ℃; Behind throttling valve throttling to 0.2～0.8MPaA, get into heat exchanger package cryogen backward channel again, for interchanger returns refrigerant compression systems after cold is provided.
Here, pressure unit MPaA is a MPa, absolute pressure.
Absorption drying system can adopt the conventional absorption drying system in this area, preferably adopts the isobaric adsorption dry flow process of following two towers or three towers, adopts molecular sieve adsorbing and dewatering, can be with moisture removal to dew points at normal pressure≤-76 ℃.
Preferably, when absorption drying system adopts two towers equipressure adsorption dry flow process:
From the Sweet natural gas after the preparatory dehydration at Sweet natural gas water distributing can top,, at first be divided into the two-way air-flow through the access road of absorption drying system; Wherein first via gas is as first adsorption tower or second adsorption tower of the direct place to go of process gas in drying process; Hocket adsorption process and regenerative process of first adsorption tower and second adsorption tower wherein; Be in the sorbent material that loads in the adsorption tower of drying process the water adsorption in the gas is got off, the gas that is not adsorbed removes the exit passageway of absorption drying system;
The second road gas gets into regenerative process as resurgent gases, and wherein the regenerative process of adsorption tower comprises thermal regeneration and two steps of cold blowing; In the thermal regeneration step, this second road gas heater via be warming up to for example 200-300 ℃ of certain temperature (preferred 210-280 ℃, more preferably 220-260 ℃; Further preferred about 240 ℃ again) after; Be used for heating and need regenerated second adsorption tower or first adsorption tower, sorbent material is heated up, moisture wherein is able to desorb; Stripping gas mixes with first via gas behind cooling and separatory again, and drying is carried out in the adsorption tower of drying process in the place to go then; In the cold blowing process; From second adsorption tower or first adsorption tower of the direct place to go of the regeneration gas of process gas in regenerative process; The adsorption tower temperature is reduced to normal temperature; Regeneration gas mixes with another road gas as process gas behind cooling and separatory then, and drying is carried out in first adsorption tower or second adsorption tower of drying process in the place to go at last.
Preferably, when absorption drying system adopts three towers equipressure adsorption dry flow process:
From the Sweet natural gas after the preparatory dehydration at Sweet natural gas water distributing can top,, at first be divided into the two-way air-flow through the access road of absorption drying system; Wherein first via gas is as first adsorption tower or second adsorption tower of the direct place to go of process gas in drying process; Hocket adsorption process and regenerative process of first adsorption tower and second adsorption tower wherein; Be in the sorbent material that loads in the adsorption tower of drying process the water adsorption in the gas is got off, the gas that is not adsorbed removes the exit passageway of absorption drying system;
The second road gas gets into regenerative process as resurgent gases, and wherein the regenerative process of adsorption tower comprises thermal regeneration and two steps of cold blowing; In the thermal regeneration step; This second road gas at first carries out drying through the 3rd adsorption tower, then heater via be warming up to for example 200-300 ℃ of certain temperature (preferred 210-280 ℃, more preferably 220-260 ℃; Further preferred about 240 ℃ again) after; Be used for heating and need regenerated second adsorption tower or the first absorption Tata, sorbent material is heated up, moisture wherein is able to desorb; Stripping gas mixes with first via gas behind cooling and separatory again, and drying is carried out in the adsorption tower of drying process in the place to go then; In the cold blowing process; From second adsorption tower or first adsorption tower of the direct place to go of the regeneration gas of process gas in regenerative process; The adsorption tower temperature is reduced to normal temperature, and then remove said the 3rd adsorption tower after the heater via heating, the sorbent material in the 3rd adsorption tower is carried out heat drying; Regeneration gas mixes with another road gas as process gas behind cooling and separatory then, and drying is carried out in first adsorption tower or second adsorption tower of drying process in the place to go at last.
The use of heavy hydrocarbon separator 3 can remove the heavy hydrocarbon component; The above heavy hydrocarbon component of C6 and C6 for example, for example the above heavy hydrocarbon component of C6 and C6 be removed to≤217ppm (preferably≤200ppm, more preferably≤100ppm; Further preferably≤50ppm, most preferably≤10ppm).
In a preferred embodiment; Wherein absorption drying system adopts two towers or the isobaric adsorption dry technology of three towers; Wherein each drying tower has at least one independently; 32 at the most, preferred 2-16, more preferably 4-16, further preferred 6-14, further preferred 8-12 adsorbent bed or composite bed still.Each sorbent material composite bed of each drying tower loads one or both or the multiple sorbent material that is selected from 3A or 4A molecular sieve, activated alumina, gac and the water-fast silica gel independently; Wherein 3A molecular sieve, 4A molecular sieve or activated alumina are as dehydrated adsorbent, and gac or water-fast silica gel are as taking off the heavy hydrocarbon sorbent material.If only load one or two or a plurality of (2-16 for example of adsorption moisture in the drying tower; Preferred 3-12, more preferably 3-8, more preferably 4-6) adsorbent bed (for example 3A molecular sieve, 4A molecular sieve or activated alumina), then implement heavy hydrocarbon separately and remove by the heavy hydrocarbon separator; And if load one or two or a plurality of (2-16 for example of adsorption moisture in the drying tower simultaneously; Preferred 3-12, more preferably 3-8, more preferably 4-6) adsorbent bed (for example 3A molecular sieve, 4A molecular sieve or activated alumina) and absorption heavy hydrocarbon one or two or a plurality of (for example 2-16 is individual; Preferred 3-12, more preferably 3-8, more preferably 4-6) adsorbent bed (gac or water-fast silica gel), then combine and implement heavy hydrocarbon and remove by adsorbent bed with the follow-up heavy hydrocarbon separator of absorption heavy hydrocarbon.Further preferably, each adsorption tower (or drying tower) has at least one the molecular sieve adsorbent bed layer and optional at least one acticarbon bed that is used to take off heavy hydrocarbon that is used to dewater; Preferred each adsorption tower has 2-16, preferred 3-12, more preferably 3-8 of being used to dewater, more preferably 2-16, preferred 3-12 of heavy hydrocarbon, more preferably individual, more preferably 4-6 acticarbon bed of 3-8 are taken off in 4-6 molecular sieve adsorbent bed layer and optional being used to.
Further preferably; Wherein absorption drying system is operated in such a way: after depickling is handled, be rich in methane blended gas separated into two parts; A part gets into drying process as process gas flow; Another part gets into step for regeneration as resurgent gases, and the mixed gas that is rich in methane that gets into drying process removes the moisture in the gas and randomly removes C6 and the above heavy hydrocarbon of C6 through drying treatment in drying tower sorbent material composite bed; Moisture removal to dew points at normal pressure≤-76 ℃ wherein, optional being removed to≤217ppm of heavy hydrocarbon component that C6 and C6 are above; The gas of the methane rich of entering step for regeneration is as the regeneration gas of drying tower regenerative process, after the completion regenerative process, in this partial regeneration gas retrieval system process gas flow.
Further preferably, wherein absorption drying system is operated in such a way:
The mixed gas that is rich in methane after depickling is handled at first is divided into the two-way air-flow through regulating valve (V1); Wherein first via gas is as first drying tower (T1) or second drying tower (T2) of the direct place to go of process gas in drying process; Hocket drying process and regenerative process of first drying tower and second drying tower wherein; The siccative that is in the middle filling of drying tower (T1 or T2) of drying process gets off the water adsorption in the gas and chooses the heavy hydrocarbon sorbent material that loads wantonly the heavy hydrocarbon in the gas is absorbed; Product gas dew points at normal pressure≤-76 after drying treatment ℃, the above heavy hydrocarbon component of C6 and C6 randomly is removed to≤217ppm;
The second road gas gets into regenerative process as resurgent gases, and wherein the regenerative process of drying tower comprises thermal regeneration and two steps of cold blowing, in the thermal regeneration step; This second road gas at first carries out drying through the 3rd drying tower (T3), then heater via (E1) be warming up to for example 200-300 ℃ (preferred 210-280 ℃, more preferably 220-260 ℃; Further preferred about 240 ℃ again) after; Heating needs regenerated drying tower (T2 or T1), and sorbent material is heated up, and moisture wherein and heavy hydrocarbon are able to desorb; Stripping gas mixes with first via gas as virgin gas behind cooling (E2) and separatory (T4) again, and drying is carried out in the drying tower of drying process in the place to go then; In the cold blowing process; From second drying tower (T2) or first drying tower (T1) of the direct place to go of the regeneration gas of process gas in regenerative process; The drying tower temperature is reduced to normal temperature, and then remove said the 3rd drying tower (T3) after the heater via heating, the sorbent material in the 3rd drying tower is carried out heat drying; Regeneration gas mixes with another road gas as process gas behind cooling (E2) and separatory (T4) then, and drying is carried out in first drying tower or second drying tower of drying process in the place to go at last.
In a preferred implementation; Its absorption drying system adopts two towers or the isobaric adsorption dry technology of three towers composite dewatering to take off heavy hydrocarbon; Each adsorption tower has at least one the molecular sieve adsorbent bed layer that is used to dewater and at least one the acticarbon bed that is used to take off heavy hydrocarbon; Two kinds of bed sums generally be two (they being that each has one), three, four (for example two molecular sieve beds and two active carbon beds), five (for example two molecular sieve beds and three active carbon beds), six, seven, eight, nine, ten, 11,12,13,14,15 or 16, or even 32.
In another preferred implementation, through the Sweet natural gas after the absorption drying system dehydration get into follow-up be the taking off the heavy hydrocarbon purification system and remove heavy hydrocarbon of sorbent material with gac etc. after, get into the liquefaction of ice chest system again.
Adopt except that the said mix refrigerant circulation technology of this patent flow process, for ice chest provides the device of the technical process of cold, also belong to the protection domain of this patent.
That is, all ice chest precooling virgin gass that relates to dewater in advance, through the device of the smart technical process of dewatering of absorption drying system, all belong to this patent protection domain again.
The advantage of the utility model:
The utility model institute adopting process flow process is at first sent virgin gas in the ice chest precooling to 5 ℃～20 ℃; This method can be sloughed the above moisture of 70wt% in the virgin gas; More than the preferred 80wt%, more preferably more than the 85wt%, the above moisture of preferred especially 90wt%; Thereby can significantly reduce the load of Sweet natural gas dehumidification system, reduce the drying plant size and reduce the sorbent material consumption.
After processing through the heavy hydrocarbon separator, the heavy hydrocarbon component, for example the above heavy hydrocarbon component of C6 and C6 is removed basically.The above heavy hydrocarbon component of C6 and C6 is removed to≤and 217ppm (preferred≤200ppm, more preferably≤100ppm, further preferred≤50ppm, most preferably≤10ppm).
In addition, if adopt two towers or three tower absorption drying systems, then also have following advantage:
If 2 utilize composite bed to remove moisture and heavy hydrocarbon simultaneously, facility investment expense and later stage system energy consumption have been reduced.The compound heavy hydrocarbon technology of taking off of drying and dehydrating of from the mixed gas that is rich in methane, producing natural gas liquids of the present invention; Make the present invention simpler and reach good decontamination effect improving than common process route; And reduced the scavenging process energy consumption, and each unit operation index is more clear, be prone to control.
3, adopt isobaric drying and dehydrating to take off heavy hydrocarbon, the almost operation under same pressure of the absorption of drying tower, heating and cooling process, the life-span of having improved program-controlled valve.
4, resurgent gases does not need independent pure gas but adopting process gas, and flow process is simple, owing to be an independently system, the start-stop car is convenient simultaneously.
5, the above heavy hydrocarbon component of C6 and C6 be removed to≤217ppm (preferred≤200ppm, more preferably≤100ppm, further preferred≤50ppm, preferred≤30ppm further, further preferred≤20ppm again, most preferably≤10ppm).
In addition,
If 6 adopt three-column process flows, can be during cold blowing with the transfer of heat of the drying tower that has heated to next tower, system energy consumption is low.
In addition; Heavy hydrocarbon separator and in drying tower, take off the heavy hydrocarbon sorbent material for example gac or combining of water-fast silica gel make C6 and the heavy hydrocarbon component more than the C6 be removed more thorough; Generally be removed to≤217ppm, preferably extremely≤200ppm, more preferably≤100ppm; Further preferably≤50ppm, most preferably≤10ppm.
Technology of the utility model or device be through adopting two towers or three tower adsorption dry flow processs, can be with the moisture removal in the Sweet natural gas to dew points at normal pressure≤-76 ℃, and preferred≤-78 ℃, more preferably≤-80 ℃.
Description of drawings
Fig. 1 is the process flow diagram of prior art;
Fig. 2 is the layout diagram of the said device of the utility model.
Fig. 3 is the schema that the composite dewatering as absorption drying system of the utility model takes off the heavy hydrocarbon process unit.
Embodiment
Further specify below in conjunction with accompanying drawing.
Device shown in Figure 2 comprises absorption drying system, refrigerant compression systems and ice chest system,
Wherein refrigerant compression systems has: a liquid phase cryogen exit passageway, a gas phase cryogen exit passageway and an access road;
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group 1; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth; Said first heat exchanger channels is connected with gas phase cryogen exit passageway with the liquid phase cryogen exit passageway of said refrigerant compression systems respectively via two pipelines with second heat exchanger channels, is connected with the access road of said refrigerant compression systems with the 3rd heat exchanger channels;
First throttling set 41 that is connected with the 3rd heat exchanger channels with first heat exchanger channels of said plate-fin heat exchanger group 1;
Second throttling set 42 that is connected with the 3rd heat exchanger channels with second heat exchanger channels of said plate-fin heat exchanger group 1; With
With a heat exchanger channels of said plate-fin heat exchanger group 1 is the Sweet natural gas water distributing can 2 that the 4th heat exchanger channels is connected,
Inlet end is the Sweet natural gas heavy hydrocarbon separator 3 that the 5th heat exchanger channels is connected with another heat exchanger channels of said plate-fin heat exchanger group 1;
The pipeline that is used for transferring raw material gas is connected to Sweet natural gas water distributing can 2 through above-mentioned the 4th heat exchanger channels of heat exchanger package 1; Sweet natural gas water distributing can 2 top gas phase ends connect an access road of absorption drying system; An exit passageway of absorption drying system connects the inlet of the 5th heat exchanger channels of plate-fin heat exchanger group 1 in the ice chest; The outlet of the 5th heat exchanger channels is connected to heavy hydrocarbon separator 3, and the heat exchanger channels that the top gas phase end of heavy hydrocarbon separator 3 passes through heat exchanger package 1 is a cooling box behind the 6th heat exchanger channels.
In addition, the top gas phase end of heavy hydrocarbon separator 3 successively through behind the 6th heat exchanger channels of heat exchanger package 1 further through cooling box behind other the 7th heat exchanger channels of heat exchanger package 1.
Absorption drying system can adopt conventional absorption drying system (for example transformation absorption drying system), preferably adopts the isobaric adsorption dry flow process of two towers or three towers, adopts molecular sieve adsorbing and dewatering, can be with moisture removal to dew points at normal pressure≤-76 ℃.Preferably, as shown in Figure 3, the absorption drying system of the utility model (the compound device that takes off heavy hydrocarbon of drying and dehydrating) comprising:
First drying tower (T1) and second drying tower (T2), the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (T3) (that is, the drying aid tower),
Well heater (E1),
Gas-liquid separator (T4) and
Water cooler (E2),
Each drying tower has one or two or a plurality of sorbent material composite bed, 3-20 bed for example, and 4-18 bed, 5-16 bed, 6-14 bed or 8-12 bed,
The transfer lime of the gas that is rich in methane after the depickling (virgin gas or process gas) is divided into two branch roads i.e. first branch road and second branch road, and first valve V1 wherein is set on first branch road; After first valve V1, divide three the tunnel to lead to liquefaction system via ingress pipe (ingress pipe when referring to that this tower is in drying process), the first drying tower T1 and the 3rd valve V3 of second valve V2, the first drying tower T1 respectively again; Ingress pipe, the second drying tower T2 and the 5th valve V5 via the 4th valve V4, the second drying tower T2 lead to liquefaction system, and are connected to the derivation port of water cooler E2 via the ingress pipe of the delivery line of optional valve (not shown), gas-liquid separator T4, gas-liquid separator T4, gas-liquid separator T4; Above-mentioned second branch road is connected to the ingress pipe of water cooler E2 respectively via the tenth valve V10 and the 11 valve V11 with via the 12 valve V12 and the 13 valve V13; Between first drying tower T1 and the 3rd valve V3, draw arm and between second drying tower T2 and the 5th valve V5, draw arm; These two arms are respectively via converging an end (port or lower port) that is connected to well heater E1 after the 8th valve V8 and the 9th valve V9; The other end of well heater is connected to the end (port or lower port) of the 3rd drying tower T3, the other end of drying tower T3 via pipe connection on the pipeline between the 12 valve V12 and the 13 the valve V13; Between first drying tower T1 and second valve V2, draw arm and between second drying tower (T2) and the 4th valve (V4), draw arm, these two arms are connected on the pipeline between the tenth valve V10 and the 11 valve V11 via converging after the 6th valve V6 and the 7th the valve V7 respectively.
The technical process of the device of use Fig. 2 is following:
Raw natural gas after the depickling at first gets in the plate-fin heat exchanger group 1 in the ice chest and carries out precooling; Cooling box after being cooled to 5 ℃～20 ℃; Get into Sweet natural gas water distributing can 2 and slough moisture from pot bottom; Sweet natural gas water distributing can 2 top gas phases continue to get into the absorption drying systems dehydration, and the Sweet natural gas after the dehydration gets into heavy hydrocarbon separator 3 and carries out gas-liquid separation after returning and being cooled to-30 ℃～-60 ℃ in the follow-up interchanger of heat exchanger package 1; Heavy hydrocarbon separator 3 bottoms obtain heavy hydrocarbon; Continue to get into all the other interchanger at different levels of heat exchanger package 1 by the isolated vapor phase stream thigh in heavy hydrocarbon separator 3 tops, and cooling box after being cooled to-130 ℃～-166 ℃ therein, natural gas liquids (LNG) obtained.
Refrigeration agent circulation technology flow process:
Refrigerant compression systems adopts C1～C5 and N
2(N for example
2: 5mol%-25mol%, C1:10mol%-25mol%, C2:30mol%-55mol%; C3:10mol%-25mol%; C5:10mol%-25mol% is based on the total mole number of whole refrigerant gas) mixing medium formed is as refrigeration agent, and the liquid phase refrigerant that comes from refrigerant compression systems at first gets into first heat exchanger channels of heat exchanger package 1; Therein by-30 ℃～-80 ℃ extremely approximately of precoolings; Behind throttling valve 41 throttlings to 0.2～0.8MPaA, get into the cryogen backward channel (i.e. the 3rd heat exchanger channels) of heat exchanger package 1, converge, for heat exchanger package 1 provides cooling box behind the cold with the refrigeration agent stream thigh that returns from heat exchanger package 1 follow-up interchanger; By refrigerant compression systems come second heat exchanger channels of gas phase refrigeration through heat exchanger package 1 be cooled to-135 ℃～-169 ℃; Behind throttling valve 42 throttlings to 0.2～0.8MPaA, get into the cryogen backward channel of heat exchanger package 1 again, for heat exchanger package 1 is returned refrigerant compression systems after cold is provided.
Here, pressure unit MPaA is a MPa, absolute pressure.
Absorption drying system can adopt conventional adsorption dry flow process (for example transformation adsorption dry flow process), preferably adopts the isobaric adsorption dry flow process of two towers or three towers, adopts molecular sieve adsorbing and dewatering, can be with moisture removal to dew points at normal pressure≤-76 ℃.
Preferably, when absorption drying system adopts two towers equipressure adsorption dry flow process:
From the Sweet natural gas after the preparatory dehydration at Sweet natural gas water distributing can top,, at first be divided into the two-way air-flow through the access road of absorption drying system; Wherein first via gas is as first adsorption tower or second adsorption tower of the direct place to go of process gas in drying process; Hocket adsorption process and regenerative process of first adsorption tower and second adsorption tower wherein; Be in the sorbent material that loads in the adsorption tower of drying process the water adsorption in the gas is got off, the gas that is not adsorbed removes the exit passageway of absorption drying system;
The second road gas gets into regenerative process as resurgent gases, and wherein the regenerative process of adsorption tower comprises thermal regeneration and two steps of cold blowing; In the thermal regeneration step; After this second road gas heater via is warming up to certain temperature; Be used for heating and need regenerated second adsorption tower or first adsorption tower, sorbent material is heated up, moisture wherein is able to desorb; Stripping gas mixes with first via gas behind cooling and separatory again, and drying is carried out in the adsorption tower of drying process in the place to go then; In the cold blowing process; From second adsorption tower or first adsorption tower of the direct place to go of the regeneration gas of process gas in regenerative process; The adsorption tower temperature is reduced to normal temperature; Regeneration gas mixes with another road gas as process gas behind cooling and separatory then, and drying is carried out in first adsorption tower or second adsorption tower of drying process in the place to go at last.
Preferably, when absorption drying system adopted the isobaric adsorption dry flow process of three towers, 3 explanation drying and dehydratings are compound with reference to the accompanying drawings took off the heavy hydrocarbon technical process:
From the Sweet natural gas after the preparatory dehydration at Sweet natural gas water distributing can top,, at first be divided into the two-way air-flow through the access road of absorption drying system; Wherein first via gas is as first adsorption tower or second adsorption tower of the direct place to go of process gas in drying process; Hocket adsorption process and regenerative process of first adsorption tower and second adsorption tower wherein; Be in the sorbent material that loads in the adsorption tower of drying process the water adsorption in the gas is got off, the gas that is not adsorbed removes the exit passageway of absorption drying system;
The second road gas gets into regenerative process as resurgent gases, and wherein the regenerative process of adsorption tower comprises thermal regeneration and two steps of cold blowing; In the thermal regeneration step; This second road gas at first carries out drying through the 3rd adsorption tower, after heater via is warming up to certain temperature then, is used for heating and needs regenerated second adsorption tower or the first absorption Tata; Sorbent material is heated up; Moisture wherein is able to desorb, and stripping gas mixes with first via gas behind cooling and separatory again, and drying is carried out in the adsorption tower of drying process in the place to go then; In the cold blowing process; From second adsorption tower or first adsorption tower of the direct place to go of the regeneration gas of process gas in regenerative process; The adsorption tower temperature is reduced to normal temperature, and then remove said the 3rd adsorption tower after the heater via heating, the sorbent material in the 3rd adsorption tower is carried out heat drying; Regeneration gas mixes with another road gas as process gas behind cooling and separatory then, and drying is carried out in first adsorption tower or second adsorption tower of drying process in the place to go at last.
The compound device (being absorption drying system) that takes off heavy hydrocarbon of drying and dehydrating is made up of three drying tower T1, T2 and T3, a well heater E1, a water cooler E2, a gas-liquid separator T4; Two is dryer tower T1, T2 in three drying towers, a drying aid tower T3; Dryer tower drying and regeneration hocket; Regeneration divides heating and cooling two steps; Product gas dew points at normal pressure≤-76 after dry composite is taken off heavy hydrocarbon ℃ are (preferred≤-78 ℃; More preferably≤-80 ℃), the above heavy hydrocarbon component of C6 and C6 is removed to≤217ppm (preferred≤200ppm, more preferably≤100ppm; Further preferably≤50ppm, most preferably≤10ppm).
The compound heavy hydrocarbon technology of taking off of isobaric drying and dehydrating, resurgent gases adopting process gas returns process gas after regenerative process, compare traditional technology, has reduced the process gas loss, has improved the liquefied fraction of gas; The compound heavy hydrocarbon unit that takes off of drying and dehydrating adopts the sorbent material composite bed, removes moisture and heavy hydrocarbon simultaneously, has reduced facility investment expense and later stage system energy consumption; The almost operation under same pressure of the absorption of its drying tower, heating and cooling process has improved equipment life.。
Be adsorbed as example with drying tower T1, its operating process is described at present:
The methane rich gas mixture that removes behind the sour gas at first is divided into two-way, and the flow of two-way air-flow is regulated through regulating valve V1: the one tunnel as resurgent gases, and one the tunnel as mainstream gas.Wherein mainstream gas is directly removed drying tower T1 through valve V2, and siccative that loads among the drying tower T1 and heavy hydrocarbon remove agent moisture in the gas and heavy hydrocarbon are absorbed, and gas is accomplished to purify through valve V3 and gone postorder liquefaction operation.
Another drying tower T2 is in regenerative process, and the regenerative process of drying tower T2 comprises heating and two steps of cold blowing:
In the thermal regeneration step; Resurgent gases is successively through valve V12, drying tower T3, well heater E1, valve V9, drying tower T2, valve V7, valve V11, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T1 that is in adsorption process again; Get into the drying tower T1 that is in adsorption process through valve V2, accomplish heat-processed drying tower T2.
Resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.When drying tower T2 was heated, regeneration gas cooled off predrying tower T3, drying tower T3 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduced the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T2, and super-dry tower T3 is predrying, and the moisture content in the resurgent gases is (moisture content in the virgin gas has reduced 80-99% usually) seldom, reduces the drying load of drying tower T2.
In the cold blowing step; Resurgent gases is successively through valve V10, valve V7, drying tower T2, valve V9, well heater E1, drying tower T3, valve V13, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T1 that is in adsorption process again; Be among the drying tower T1 of adsorption process through valve V2 entering, accomplish process of cooling drying tower T2.
Equally, resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.Drying tower T2 is being carried out refrigerative simultaneously, regeneration gas heats predrying tower T3, drying tower T2 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduces the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T3, and super-dry tower T2 is predrying, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T3.
Drying tower T2 waits for getting into adsorption operations next time through after the above-mentioned heating and cooling process.
The regenerative process of the regenerative process of drying tower T1 and drying tower T2 is just the same, just needs the valve numbering of action different.Two drying towers replace absorption regeneration, realize operate continuously processing gas.
The composite bed of each drying tower can load in 3A or the sorbent materials such as 4A molecular sieve, activated alumina, gac and silica gel one or both or multiple.
Then, T2 is adsorbed as example with drying tower, and its operating process is described:
The gas mixture that removes the methane rich behind the sour gas at first is divided into two-way, and the flow of two-way air-flow is regulated through regulating valve V1: the one tunnel as resurgent gases, and one the tunnel as mainstream gas.Wherein mainstream gas is directly removed drying tower T2 through valve V4, and siccative that loads among the drying tower T2 and heavy hydrocarbon remove agent moisture in the gas and heavy hydrocarbon are absorbed, and gas is accomplished to purify through valve V5 and gone postorder liquefaction operation.
Another drying tower T1 is in regenerative process, and the regenerative process of drying tower T1 comprises heating and two steps of cold blowing:
In the thermal regeneration step; Resurgent gases is successively through valve V12, drying tower T3, well heater E1, valve V8, drying tower T1, valve V6, valve V11, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T2 that is in adsorption process again; Get into the drying tower T2 that is in adsorption process through valve V4, accomplish heat-processed drying tower T1.
Resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.When drying tower T1 was heated, regeneration gas cooled off predrying tower T3, drying tower T3 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduced the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T1, and it is predrying to have passed through predrying tower T3, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T1.
In the cold blowing step; Resurgent gases is successively through valve V10, valve V6, drying tower T1, valve V8, well heater E1, drying tower T3, valve V13, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T2 that is in adsorption process again; Get into the drying tower T2 that is in adsorption process through valve V4, accomplish process of cooling drying tower T1.
Equally, resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.Drying tower T1 is being carried out refrigerative simultaneously, regeneration gas heats predrying tower T3, drying tower T1 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduces the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T3, and super-dry tower T1 is predrying, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T3.
Drying tower T1 waits for getting into adsorption operations next time through after the above-mentioned heating and cooling process.
Preferably; Absorption drying system adopts two towers or the isobaric adsorption dry technology of three towers composite dewatering to take off heavy hydrocarbon; Each adsorption tower (or drying tower) has at least one the molecular sieve adsorbent bed layer that is used to dewater and at least one the acticarbon bed that is used to take off heavy hydrocarbon; Two kinds of bed sums generally be two (they being that each has one), three, four (for example two molecular sieve beds and two active carbon beds), five (for example two molecular sieve beds and three active carbon beds), six, seven, eight, nine, ten, 11,12,13,14,15 or 16, or even 32.
Randomly, through the Sweet natural gas after the absorption drying system dehydration can get into follow-up be the taking off the heavy hydrocarbon purification system and remove heavy hydrocarbon of sorbent material with gac etc. after, get into the liquefaction of ice chest system again.
Adopt except that the said mix refrigerant circulation technology of this patent flow process, for ice chest provides the device of the technical process of cold, also belong to the protection domain of this patent.
That is, all ice chest precooling virgin gass that relates to dewater in advance, through the device of the smart technical process of dewatering of absorption drying system, all belong to this patent protection domain again.
Claims (6)
1. Sweet natural gas drying and liquefying plant is characterized in that this device comprises absorption drying system, refrigerant compression systems and ice chest system,
Wherein refrigerant compression systems has: a liquid phase cryogen exit passageway, a gas phase cryogen exit passageway and an access road;
Wherein the ice chest system comprises:
One group of plate-fin heat exchanger group; It comprises at least six heat exchanger channels: the 5th and the 6th heat exchanger channels first, second, third, fourth; Said first heat exchanger channels is connected with gas phase cryogen exit passageway with the liquid phase cryogen exit passageway of said refrigerant compression systems respectively via two pipelines with second heat exchanger channels, is connected with the access road of said refrigerant compression systems with the 3rd heat exchanger channels;
First throttling set that is connected with the 3rd heat exchanger channels with first heat exchanger channels of said plate-fin heat exchanger group;
Second throttling set that is connected with the 3rd heat exchanger channels with second heat exchanger channels of said plate-fin heat exchanger group;
With
With a heat exchanger channels of said plate-fin heat exchanger group is the Sweet natural gas water distributing can that the 4th heat exchanger channels is connected,
Inlet end is the Sweet natural gas heavy hydrocarbon separator that the 5th heat exchanger channels is connected with another heat exchanger channels of said plate-fin heat exchanger group;
The pipeline that is used to carry Sweet natural gas after the depickling is connected to the Sweet natural gas water distributing can through above-mentioned the 4th heat exchanger channels of heat exchanger package; Sweet natural gas water distributing can top gas phase end connects an access road of absorption drying system; An exit passageway of absorption drying system connects the inlet of the 5th heat exchanger channels of plate-fin heat exchanger group in the ice chest; The outlet of the 5th heat exchanger channels is connected to the heavy hydrocarbon separator, and the heat exchanger channels that the top gas phase end of heavy hydrocarbon separator passes through heat exchanger package is a cooling box behind the 6th heat exchanger channels.
2. Sweet natural gas drying according to claim 1 and liquefying plant is characterized in that, the top gas phase end of heavy hydrocarbon separator successively through behind the 6th heat exchanger channels of heat exchanger package further through cooling box behind other the 7th heat exchanger channels of heat exchanger package.
3. Sweet natural gas drying according to claim 1 and liquefying plant is characterized in that, through the Sweet natural gas after the absorption drying system dehydration get into follow-up be the taking off the heavy hydrocarbon purification system and remove heavy hydrocarbon of sorbent material with the gac after, get into the liquefaction of ice chest system again.
4. according to each described Sweet natural gas drying and liquefying plant of claim 1-3, it is characterized in that said absorption drying system adopts two towers or the isobaric absorption drying system of three towers.
5. Sweet natural gas drying according to claim 4 and liquefying plant is characterized in that absorption drying system comprises:
First drying tower (T1) and second drying tower (T2), the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (T3),
Well heater (E1),
Gas-liquid separator (T4) and
Water cooler (E2),
Each drying tower has one or two or a plurality of sorbent material composite bed,
The transfer of gas pipe that is rich in methane after the depickling is divided into two branch roads i.e. first branch road and second branch road, and first valve (V1) wherein is set on first branch road; Divide three the tunnel to lead to liquefaction system via ingress pipe, the first drying tower T1 and the 3rd valve (V3) of second valve (V2), first drying tower (T1) respectively afterwards again at first valve (V1); Ingress pipe, second drying tower (T2) and the 5th valve (V5) via the 4th valve (V4), second drying tower (T2) lead to liquefaction system, and are connected to the derivation port of water cooler (E2) via the ingress pipe of the delivery line of optional valve, gas-liquid separator (T4), gas-liquid separator (T4), gas-liquid separator (T4); Above-mentioned second branch road is connected to the ingress pipe of water cooler (E2) respectively via the tenth valve (V10) and the 11 valve (V11) with via the 12 valve (V12) and the 13 valve (V13); Draw arm between first drying tower (T1) and the 3rd valve (V3) and between second drying tower (T2) and the 5th valve (V5), drawing arm; These two arms converge an end that is connected to well heater (E1) via the 8th valve (V8) and the 9th valve (V9) respectively afterwards; The other end of well heater is connected to an end of the 3rd drying tower (T3), the other end of drying tower (T3) via pipe connection on the pipeline between the 12 valve (V12) and the 13 valve (V13); Drawing arm between first drying tower (T1) and second valve (V2) and between second drying tower (T2) and the 4th valve (V4), drawing arm, these two arms converge afterwards via the 6th valve (V6) and the 7th valve (V7) respectively and are connected on the pipeline between the tenth valve (V10) and the 11 valve (V11).
6. Sweet natural gas drying according to claim 5 and liquefying plant; It is characterized in that; Each sorbent material composite bed of each drying tower loads a kind of sorbent material that is selected from 3A or 4A molecular sieve, activated alumina, gac and the water-fast silica gel independently; Wherein 3A molecular sieve, 4A molecular sieve or activated alumina are as dehydrated adsorbent, and gac or water-fast silica gel are as taking off the heavy hydrocarbon sorbent material.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102643694A (en) * | 2012-04-27 | 2012-08-22 | 新地能源工程技术有限公司 | Technique and device for drying and liquefaction of natural gas |
| CN106839649A (en) * | 2017-02-13 | 2017-06-13 | 重庆耐德能源装备集成有限公司 | The liquefying device and method of a kind of natural gas |
| CN108645117A (en) * | 2018-05-30 | 2018-10-12 | 科霖恩新能源科技（江苏）有限公司 | A kind of natural gas liquefaction ice chest of integrated carbon dioxide separation module |
| CN110145458A (en) * | 2019-06-21 | 2019-08-20 | 蚌埠隆华压铸机有限公司 | It is a kind of with well remove moist natural gas compressor |
| CN112922580A (en) * | 2019-12-06 | 2021-06-08 | 中国石油天然气股份有限公司 | Natural gas processing system, control method thereof and natural gas transmission system |
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2012
- 2012-04-27 CN CN 201220186602 patent/CN202595073U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102643694A (en) * | 2012-04-27 | 2012-08-22 | 新地能源工程技术有限公司 | Technique and device for drying and liquefaction of natural gas |
| CN102643694B (en) * | 2012-04-27 | 2014-12-03 | 新地能源工程技术有限公司 | Technique and device for drying and liquefaction of natural gas |
| CN106839649A (en) * | 2017-02-13 | 2017-06-13 | 重庆耐德能源装备集成有限公司 | The liquefying device and method of a kind of natural gas |
| CN108645117A (en) * | 2018-05-30 | 2018-10-12 | 科霖恩新能源科技（江苏）有限公司 | A kind of natural gas liquefaction ice chest of integrated carbon dioxide separation module |
| CN108645117B (en) * | 2018-05-30 | 2024-01-19 | 科霖恩新能源科技（江苏）有限公司 | Natural gas liquefaction cold box integrated with carbon dioxide separation module |
| CN110145458A (en) * | 2019-06-21 | 2019-08-20 | 蚌埠隆华压铸机有限公司 | It is a kind of with well remove moist natural gas compressor |
| CN112922580A (en) * | 2019-12-06 | 2021-06-08 | 中国石油天然气股份有限公司 | Natural gas processing system, control method thereof and natural gas transmission system |
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