CN104073310A - Device and method for purifying and drying natural gas - Google Patents
Device and method for purifying and drying natural gas Download PDFInfo
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- CN104073310A CN104073310A CN201410339128.0A CN201410339128A CN104073310A CN 104073310 A CN104073310 A CN 104073310A CN 201410339128 A CN201410339128 A CN 201410339128A CN 104073310 A CN104073310 A CN 104073310A
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Abstract
The invention relates to a device and a method for purifying and drying natural gas. The device comprises deacidifying dehydrating beds, de-heavy-hydrocarbon beds, auxiliary pipelines and controlling valves, wherein as key processing equipment, the deacidifying dehydrating beds and the de-heavy-hydrocarbon beds adopt a shell-and-pipe structure respectively; adsorbents are packed in pipe passes as adsorbent bed layers; shell passes pass through heating media and coolants. According to the invention, when regenerated adsorbent bed layers are heated through the method, the external heating media and coolants are directly introduced into the deacidifying dehydrating beds and the de-heavy-hydrocarbon beds for heating and cooling, so that regenerated gas doesn't need to be used; the adsorbent bed layers can be completely regenerated only on the condition that a small number of carrier gas is introduced into the pipe side in the regenerating process, so that the problem that the regenerated gas is consumed so much when the conventional adsorbent bed layers are heated for regeneration can be solved, the consumption of raw natural gas is reduced, and the liquidation rate of liquefied natural gas is increased; the method is adopted, so that the energy consumption is low, the utilization rate of the raw natural gas is high, and the economy is good.
Description
Technical field
The present invention relates to gas sweetening and preprocessing technical field, particularly a kind of method of natural gas conditioning and dry gas.
Background technology
The purification of Sweet natural gas is the technological process that the heavy hydrocarbons such as the sour gas such as the carbonic acid gas in Sweet natural gas, hydrogen sulfide, moisture and the above hydro carbons of C5 are removed with being dried.Thereby avoid in gas deliquescence process during this process forming in deep cooling process, ice, solid hydrate or solid heavy hydrocarbon block or the requisite operation of damage equipment even.
The removal methods of sour gas, moisture and heavy hydrocarbon that at present, in gas deliquescence process, process gas contains comprises absorption process, absorption method, low temperature process, membrane separation process etc.Wherein sour gas remove with absorption process effect best, best to gas deep dehydration, de-heavy hydrocarbon effect with absorption method.Thereby, in existing technique, conventionally first with absorption process, remove the sour gas in Sweet natural gas, then remove moisture and the heavy hydrocarbon in Sweet natural gas with absorption process.The advantage of this technique is technology maturation, and Acidic Gas Treating load is high, good stability.But, the shortcoming of method also clearly: first amine liquid regenerative process need be heated to 115 ℃ of left and right by 40 ℃ by whole solution, and the energy consumption of reboiler is very large; Its two be Sweet natural gas humidity after acid gas removal all can with amine liquid contact process in arrive the saturated follow-up drying load amount that increased.In addition, sour gas absorption process adopts amine liquid, needs to consume aqueous solvent, limited by geographical conditions, and this method cannot be applied in place abundant at the medium gas well gas of area of Tarim in Xinjiang but lack of water.Absorption method also can be used for sour gas and removes, and this subtractive process is consistent with the technique that existing absorption method removes moisture and heavy hydrocarbon, and the method device is simple, and technique does not need aqueous solvent.Yet the method is traditional absorbing process, during regeneration adsorption bed, adopt resurgent gases, work as CO
2when content surpasses 0.5%, the regeneration tolerance consumption that bed needs is very big, will account for 50% even 100% of raw material air input.This part resurgent gases is because containing CO
2can only drain into out-of-bounds or burn, thereby causing this technique energy consumption when processing the Sweet natural gas of the acid gas of high-content too high, resurgent gases quantity not sufficient even, regeneration not exclusively, affects the normal work of downstream deep cooling operation.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, reduce resurgent gases consumption, thereby provide a kind of natural gas conditioning and dry apparatus and method, the method utilizes depickling dehydration bed and the de-heavy hydrocarbon bed of shell-and-tube to remove sour gas, water and the heavy hydrocarbon in Sweet natural gas, not only saved resurgent gases, increased unstripped gas utilization ratio, and acid gas removal and dehydration is integrated, and technique is simple.
Method of the present invention, by adopting shell-and-tube depickling dehydration bed and de-heavy hydrocarbon bed to remove sour gas, water and the heavy hydrocarbon in Sweet natural gas, specifically comprises the following steps:
1) the first depickling dehydration bed D1 is set, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2, be tube shell type structure, wherein, at the first depickling dehydration bed D1, the second depickling dehydration bed D2, the tube side side of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed is loaded sorbent material as adsorption bed, natural gas line is connected with the tube side of de-heavy hydrocarbon bed with depickling dehydration bed, refrigerant is connected with the shell side of de-heavy hydrocarbon bed with depickling dehydration bed with heating agent pipeline, wherein, the tube side of the tube side of the first depickling dehydration bed D1 and the second depickling dehydration bed D2 is connected in parallel by valve and pipeline, the shell side of the tube side of the first depickling dehydration bed D1 and the second depickling dehydration bed D2 is connected in parallel by valve and pipeline, the tube side of the tube side of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 is connected in parallel by valve and pipeline, the shell side of the shell side of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 is connected in parallel by valve and pipeline, between depickling dehydration bed and the tube side of de-heavy hydrocarbon bed, be connected in series, between depickling dehydration bed and the shell side of de-heavy hydrocarbon bed, be connected in parallel,
2) the raw material moisture that is rich in sour gas is passed into sour gas and the moisture that the tube side of the first depickling dehydration bed D1 removes in raw material moisture and obtain dry gas, the tube side that passes into afterwards the first de-heavy hydrocarbon bed C1 removes the heavy hydrocarbon in unstripped gas, the gas product after being finally purified;
3) after the first depickling dehydration bed D1 absorption is saturated, by valve, switched to reproduced state, unstripped gas passes into the tube side of the second depickling dehydration bed D2;
4) shell side that heating agent is passed into the first depickling dehydration bed D1 through the 23 valve V23 by bottom inlet carries out thermal regeneration to adsorption bed, when adsorption bed temperature reaches 100 ℃, through the 6th valve V6, to the tube side of the first depickling dehydration bed D1, passing into carrier gas blows away the sour gas parsing in adsorption bed and water vapour through the second valve V2, when bed temperature rises to 180～280 ℃, keep adsorption bed temperature 0～2 hour, stop afterwards passing into heating agent;
5) shell side that refrigerant is passed into the first depickling dehydration bed D1 through the 22 valve V22 by bottom inlet carries out cooling to adsorption bed, when adsorption bed temperature is down to 40～55 ℃, stop passing into refrigerant, stop passing into simultaneously carrier gas now a first depickling dehydration bed D1 completed regeneration, standby until enter next sorption cycle.
In above-mentioned technical scheme, after the first de-heavy hydrocarbon bed C1 absorption is saturated, by valve, switched to reproduced state, the unstripped gas after depickling dehydration passes into the second de-heavy hydrocarbon bed C2, and according to step 4) and 5) the first de-heavy hydrocarbon bed C1 is regenerated with cooling.
In above-mentioned technical scheme, if when heating agent is steam, refrigerant should be water coolant, if when heating agent is deep fat, refrigerant is also deep fat.
In above-mentioned technical scheme, step 4) and step 5) in pass into the first depickling dehydration bed D1 the dry gas of carrier gas after from flashed vapour or depickling dehydration, the gas product of the carrier gas passing into during regeneration the first de-heavy hydrocarbon bed C1 after from flashed vapour or de-heavy hydrocarbon.
In above-mentioned technical scheme, step 4) in, pass into the carrier gas of the first depickling dehydration bed D1 finally as fuel gas, step 5) carrier gas that passes into the first depickling dehydration bed D1 in enters de-heavy hydrocarbon operation together with after dry gas from the second depickling dehydration bed D2 mixes, and the carrier gas that passes into the first de-heavy hydrocarbon bed C1 is final all as fuel gas.
In above-mentioned technical scheme, the sour gas in Sweet natural gas refers to the gases such as carbonic acid gas, hydrogen sulfide, and heavy hydrocarbon refers to C5 and above hydro carbons, step 1) in sorbent material be molecular sieve, activated alumina or silica gel.
In above-mentioned technical scheme, the tube side pipe diameter used of depickling dehydration bed and de-heavy hydrocarbon bed is 50～400mm.
In above-mentioned technical scheme, depickling dehydration procedure and de-heavy hydrocarbon inter process are provided with the first reducing valve V38, the Pressure Drop of depickling dehydration bed adsorption bed when its Pressure Drop equals cooling.
The present invention also provides a kind of natural gas conditioning and dry device, comprise: depickling dehydration bed, de-heavy hydrocarbon bed and subsidiary pipeline and valve, connect successively tube side, the dry gas pipeline of raw material moisture feeding line, depickling dehydration bed, tube side and the gas product pipeline of de-heavy hydrocarbon bed, wherein, depickling dehydration bed and de-heavy hydrocarbon bed are tube shell type structure, between depickling dehydration bed, be connected in parallel, between different depickling dehydration beds, by valve, control and carry out independently of one another adsorption dry, regeneration and cooling; Between de-heavy hydrocarbon bed, also for being connected in parallel, between different de-heavy hydrocarbon beds, by valve, control and carry out independently of one another adsorption dry, regeneration and cooling; Between depickling dehydration bed and the tube side of de-heavy hydrocarbon bed, be connected in series, between depickling dehydration bed and the shell side of de-heavy hydrocarbon bed, be connected in parallel.
The tube side bottom inlet of above-mentioned depickling dehydration bed is all connected with flashed vapour pipeline with dry gas pipeline, the tube side bottom inlet of de-heavy hydrocarbon bed is all connected with flashed vapour pipeline with gas product pipeline, and depickling dehydration bed is all connected with refrigerant pipeline with heating agent with the shell side of de-heavy hydrocarbon bed.
The quantity of above-mentioned depickling dehydration bed is 2～4, and the quantity of de-heavy hydrocarbon bed is 2～3.
Technical scheme of the present invention is first by adopting shell-and-tube depickling dehydration bed to remove the acid G&W in Sweet natural gas, the de-heavy hydrocarbon bed of recycling shell-and-tube removes heavy hydrocarbon in Sweet natural gas, regenerative process relies on outside heating agent from tube side indirect heating, process of cooling relies on outside refrigerant indirectly cooling from tube side, and whole process only needs to pass into water and the CO that a small amount of carrier gas desorption when taking away regeneration produces
2, not only saved resurgent gases, increase unstripped gas utilization ratio, and realized the integrated of acid gas removal and dehydration, technique is simple, and operability is high.Adopt depickling dehydration bed and the de-heavy hydrocarbon bed shell design pressure of shell-and-tube low, facility investment is few.
Advantage of the present invention and active effect are, the method that the depickling dehydration bed of the shell-and-tube adopting and de-heavy hydrocarbon bed remove sour gas, water and heavy hydrocarbon in Sweet natural gas has realized the integrated of technological process, the mode of only adsorbing by bed can realize the purification of the Sweet natural gas of high-concentration acidic wastewater gas content, not only avoid resurgent gases consumption, increased unstripped gas utilization ratio, and simplified gas purifying process flow process, reduced investment, process cost is low, cost-saving, thereby produces obvious economic benefit.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
In figure, code name implication is as follows:
D1: the first depickling dehydration bed;
D2: the second depickling dehydration bed;
C1: the first de-heavy hydrocarbon bed;
C2: the second de-heavy hydrocarbon bed;
AR: online water analyzer;
V1～V41: valve.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is explained
Embodiment 1
The concrete technology flow process of the present embodiment refers to Fig. 1.
A kind of natural gas conditioning and dry device, the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 are set, wherein, the first depickling dehydration bed D1 and the second depickling dehydration bed D2 are connected in parallel by valve and pipeline, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 are connected in parallel by valve and pipeline, between depickling dehydration bed and the tube side of de-heavy hydrocarbon bed, be connected in series, between depickling dehydration bed and the shell side of de-heavy hydrocarbon bed, be connected in parallel; Unstripped gas feeding line connects the pipe side roof part entrance of the first depickling dehydration bed D1 and the second depickling dehydration bed D2, the pipe side bottom outlet of the first depickling dehydration bed D1 and the second depickling dehydration bed D2 is connected to the pipe side roof part entrance of line water analyzer AR, the first reducing valve V38 and the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 in turn, and the pipe side bottom outlet of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2 is connected gas product pipeline.The feeding line of refrigerant and heating agent is connected with the shell-side bottom inlet of the second de-heavy hydrocarbon bed C2 with the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1, and the discharging pipeline of refrigerant and heating agent is connected with the shell-side top exit of the second de-heavy hydrocarbon bed C2 with the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1.Flashed vapour pipeline entrance is connected with the carrier gas line of the pipe side bottom entrance of the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed C2.
The bed pipe diameter of depickling dehydration bed and de-heavy hydrocarbon bed is 300mm, in the pipe side of the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed, loads silica gel as adsorption bed.By CO2 content, be that raw material moisture that 3mol%, benzene content are 500ppmv passes into the first depickling dehydration bed D1 and removes sour gas in raw material moisture and moisture to obtain CO2 content be that 15ppmv, water-content are the dry gas that 0.5ppmv, benzene content are 500ppmv, pass into afterwards the first de-heavy hydrocarbon bed C1 and remove the heavy hydrocarbon in unstripped gas, being finally purified rear CO2 content is that 15ppmv, water-content are the gas product that 0.5ppmv, benzene content are 2ppmv.After the first depickling dehydration bed D1 absorption is saturated, by valve, switched to reproduced state, unstripped gas passes into the second depickling dehydration bed D2.The shell side that the deep fat of 300 ℃ is passed into the first depickling dehydration bed D1 by bottom inlet carries out thermal regeneration to adsorption bed, when adsorption bed temperature reaches 100 ℃, passing into carrier gas blows away the sour gas parsing in adsorption bed and water vapour, carrier gas, from flashed vapour, is carried the carrier gas of sour gas and water vapour directly as fuel gas.When bed temperature rises to 280 ℃, stop passing into deep fat, complete thermal regeneration process.The shell side that afterwards deep fat of normal temperature is passed into the first depickling dehydration bed D1 by bottom inlet carries out cooling to adsorption bed, now carrier gas enters de-heavy hydrocarbon operation by the tenth valve V10, when adsorption bed temperature is down to 55 ℃, stop passing into the deep fat of normal temperature, stop passing into simultaneously carrier gas now a first depickling dehydration bed D1 completed regeneration, standby until enter next sorption cycle.
After the first de-heavy hydrocarbon bed C1 absorption is saturated, by valve, switched to reproduced state, the unstripped gas after depickling dehydration passes into the second de-heavy hydrocarbon bed C2, with above-mentioned same operation conditions, the first de-heavy hydrocarbon bed C1 regenerate with cooling.
Embodiment 2
The concrete technology flow process of the present embodiment refers to Fig. 1.
The bed pipe diameter of the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed is 400mm, pipe side at the first depickling dehydration bed D1 and the second depickling dehydration bed D2 is loaded molecular sieve as adsorption bed, in the pipe side of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed, loads silica gel as adsorption bed.By CO2 content, be that raw material moisture that 1mol%, benzene content are 100ppmv passes into the first depickling dehydration bed D1 and removes sour gas in raw material moisture and moisture to obtain CO2 content be that 10ppmv, water-content are the dry gas that 0.6ppmv, benzene content are 100ppmv, pass into afterwards the first de-heavy hydrocarbon bed C1 and remove the heavy hydrocarbon in unstripped gas, being finally purified rear CO2 content is that 10ppmv, water-content are the gas product that 0.6ppmv, benzene content are 1ppmv.After the first depickling dehydration bed D1 absorption is saturated, by valve, switched to reproduced state, unstripped gas passes into the second depickling dehydration bed D2.The shell side that the overheated steam of 350 ℃ is passed into the first depickling dehydration bed D1 by bottom inlet carries out thermal regeneration to adsorption bed, when adsorption bed temperature reaches 100 ℃, passing into carrier gas blows away the sour gas parsing in adsorption bed and water vapour, carrier gas, from dry gas, is carried the carrier gas of sour gas and water vapour directly as fuel gas.When bed temperature rises to 230 ℃, stop passing into overheated steam, complete thermal regeneration process.The shell side that afterwards water coolant is passed into the first depickling dehydration bed D1 by bottom inlet carries out cooling to adsorption bed, now carrier gas enters de-heavy hydrocarbon operation by the tenth valve V10, when adsorption bed temperature is down to 40 ℃, stop passing into water coolant, stop passing into simultaneously carrier gas now a first depickling dehydration bed D1 completed regeneration, standby until enter next sorption cycle.
After the first de-heavy hydrocarbon bed C1 absorption is saturated, by valve, switched to reproduced state, the unstripped gas after depickling dehydration passes into the second de-heavy hydrocarbon bed C2, with above-mentioned same operation conditions, the first de-heavy hydrocarbon bed C1 regenerate with cooling.
Embodiment 3
The concrete technology flow process of the present embodiment refers to Fig. 1.
The bed pipe diameter of the first depickling dehydration bed D1, the second depickling dehydration bed D2, the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed is 50mm, pipe side at the first depickling dehydration bed D1 and the second depickling dehydration bed D2 is loaded activated alumina as adsorption bed, in the pipe side of the first de-heavy hydrocarbon bed C1 and the second de-heavy hydrocarbon bed, loads silica gel as adsorption bed.By CO2 content, be that 0.01mol%, H2S content are that raw material moisture that 50ppmv, benzene content are 20ppmv passes into the first depickling dehydration bed D1 and removes sour gas in raw material moisture and moisture to obtain CO2 content be that 20ppmv, water-content are the dry gas that 0.8ppmv, benzene content are 20ppmv, pass into afterwards the first de-heavy hydrocarbon bed C1 and remove the heavy hydrocarbon in unstripped gas, being finally purified rear CO2 content is that 20ppmv, water-content are the gas product that 0.8ppmv, benzene content are 1.6ppmv.After the first depickling dehydration bed D1 absorption is saturated, by valve, switched to reproduced state, unstripped gas passes into the second depickling dehydration bed D2.The shell side that the deep fat of 300 ℃ is passed into the first depickling dehydration bed D1 by bottom inlet carries out thermal regeneration to adsorption bed, when adsorption bed temperature reaches 100 ℃, passing into carrier gas blows away the sour gas parsing in adsorption bed and water vapour, carrier gas, from dry gas, is carried the carrier gas of sour gas and water vapour directly as fuel gas.When bed temperature rises to 180 ℃, stop passing into overheated steam, complete thermal regeneration process.The shell side that afterwards water coolant is passed into the first depickling dehydration bed D1 by bottom inlet carries out cooling to adsorption bed, now carrier gas enters de-heavy hydrocarbon operation by the tenth valve V10, when adsorption bed temperature is down to 50 ℃, stop passing into water coolant, stop passing into simultaneously carrier gas now a first depickling dehydration bed D1 completed regeneration, standby until enter next sorption cycle.
After the first de-heavy hydrocarbon bed C1 absorption is saturated, by valve, switched to reproduced state, the unstripped gas after depickling dehydration passes into the second de-heavy hydrocarbon bed C2, with above-mentioned same operation conditions, the first de-heavy hydrocarbon bed C1 regenerate with cooling.
Claims (10)
1. natural gas conditioning and a dry method, is characterized in that, the method, by adopting shell-and-tube depickling dehydration bed and de-heavy hydrocarbon bed to remove sour gas, water and the heavy hydrocarbon in Sweet natural gas, specifically comprises the following steps:
1) the first depickling dehydration bed (D1) is set, the second depickling dehydration bed (D2), the first de-heavy hydrocarbon bed (C1) and the second de-heavy hydrocarbon bed (C2), be tube shell type structure, wherein, at the first depickling dehydration bed (D1), the second depickling dehydration bed (D2), the tube side side of the first de-heavy hydrocarbon bed (C1) and the second de-heavy hydrocarbon bed is loaded sorbent material as adsorption bed, natural gas line is connected with the tube side of de-heavy hydrocarbon bed with depickling dehydration bed, refrigerant is connected with the shell side of de-heavy hydrocarbon bed with depickling dehydration bed with heating agent pipeline, wherein, the tube side of the tube side of the first depickling dehydration bed (D1) and the second depickling dehydration bed (D2) is connected in parallel by valve and pipeline, the shell side of the tube side of the first depickling dehydration bed (D1) and the second depickling dehydration bed (D2) is connected in parallel by valve and pipeline, the tube side of the tube side of the first de-heavy hydrocarbon bed (C1) and the second de-heavy hydrocarbon bed (C2) is connected in parallel by valve and pipeline, the shell side of the shell side of the first de-heavy hydrocarbon bed (C1) and the second de-heavy hydrocarbon bed (C2) is connected in parallel by valve and pipeline, between depickling dehydration bed and the tube side of de-heavy hydrocarbon bed, be connected in series, between depickling dehydration bed and the shell side of de-heavy hydrocarbon bed, be connected in parallel,
2) the raw material moisture that is rich in sour gas is passed into sour gas and the moisture that the tube side of the first depickling dehydration bed (D1) removes in raw material moisture and obtain dry gas, the tube side that passes into afterwards the first de-heavy hydrocarbon bed (C1) removes the heavy hydrocarbon in unstripped gas, the gas product after being finally purified;
3) at the first depickling dehydration bed (D1), adsorb after saturated and switched to reproduced state by valve, unstripped gas passes into the tube side of the second depickling dehydration bed (D2);
4) shell side that heating agent is passed into the first depickling dehydration bed (D1) through the 23 valve (V23) by bottom inlet carries out thermal regeneration to adsorption bed, when adsorption bed temperature reaches 100 ℃, through the 6th valve (V6), to the tube side of the first depickling dehydration bed (D1), passing into carrier gas blows away the sour gas parsing in adsorption bed and water vapour through the second valve (V2), when bed temperature rises to 180～280 ℃, keep adsorption bed temperature 0～2 hour, stop afterwards passing into heating agent;
5) shell side that refrigerant is passed into the first depickling dehydration bed (D1) through the 22 valve (V22) by bottom inlet carries out cooling to adsorption bed, when adsorption bed temperature is down to 40～55 ℃, stop passing into refrigerant, stop passing into now the first depickling dehydration bed (D1) of carrier gas simultaneously and completed regeneration, standby until enter next sorption cycle.
2. method according to claim 1, it is characterized in that, when adsorbing after saturated, the first de-heavy hydrocarbon bed (C1) switched to reproduced state by valve, unstripped gas after depickling dehydration passes into the second de-heavy hydrocarbon bed (C2), and according to step 4) and 5) the first de-heavy hydrocarbon bed (C1) is regenerated with cooling.
3. method according to claim 1, is characterized in that, if when heating agent is steam, refrigerant should be water coolant, if when heating agent is deep fat, refrigerant is also deep fat.
4. method according to claim 1, it is characterized in that, step 4) and step 5) in pass into the first depickling dehydration bed (D1) the dry gas of carrier gas after from flashed vapour or depickling dehydration, the gas product of the carrier gas passing into during regeneration the first de-heavy hydrocarbon bed (C1) after from flashed vapour or de-heavy hydrocarbon.
5. method according to claim 1, it is characterized in that, step 4) in, pass into the carrier gas of the first depickling dehydration bed (D1) finally as fuel gas, step 5) carrier gas that passes into first depickling dehydration bed (D1) tube side in enters de-heavy hydrocarbon operation together with after dry gas from second depickling dehydration bed (D2) tube side mixes, and the carrier gas that passes into the first de-heavy hydrocarbon bed (C1) tube side is final all as fuel gas.
6. method according to claim 1, is characterized in that, the sour gas in Sweet natural gas refers to the gases such as carbonic acid gas, hydrogen sulfide, and heavy hydrocarbon refers to C5 and above hydro carbons, step 1) in sorbent material be molecular sieve, activated alumina or silica gel.
7. method according to claim 1, is characterized in that, the tube side pipe diameter used of depickling dehydration bed and de-heavy hydrocarbon bed is 50～400mm.
8. a natural gas conditioning and dry device, comprise: depickling dehydration bed, de-heavy hydrocarbon bed and subsidiary pipeline and valve, connect successively tube side, the dry gas pipeline of raw material moisture feeding line, depickling dehydration bed, tube side and the gas product pipeline of de-heavy hydrocarbon bed, wherein, depickling dehydration bed and de-heavy hydrocarbon bed are tube shell type structure, between depickling dehydration bed, be connected in parallel, between different depickling dehydration beds, by valve, control and carry out independently of one another adsorption dry, regeneration and cooling; Between de-heavy hydrocarbon bed, also for being connected in parallel, between different de-heavy hydrocarbon beds, by valve, control and carry out independently of one another adsorption dry, regeneration and cooling; Between depickling dehydration bed and the tube side of de-heavy hydrocarbon bed, be connected in series, between depickling dehydration bed and the shell side of de-heavy hydrocarbon bed, be connected in parallel.
9. natural gas conditioning according to claim 8 and dry device, it is characterized in that, the tube side bottom inlet of depickling dehydration bed is all connected with flashed vapour pipeline with dry gas pipeline, the tube side bottom inlet of de-heavy hydrocarbon bed is all connected with flashed vapour pipeline with gas product pipeline, and depickling dehydration bed is all connected with refrigerant pipeline with heating agent with the shell side of de-heavy hydrocarbon bed.
10. natural gas conditioning according to claim 8 and dry device, is characterized in that, the quantity of depickling dehydration bed is 2-4, and the quantity of de-heavy hydrocarbon bed is 2～3.
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| CN105779056B (en) * | 2016-05-16 | 2018-11-30 | 重庆耐德能源装备集成有限公司 | A kind of natural gas removing system and its regenerating unit |
| CN105969440A (en) * | 2016-06-29 | 2016-09-28 | 长春汽车燃气发展有限公司 | Natural gas desulfurization device with desulfurizer regeneration function |
| CN107216923A (en) * | 2017-06-27 | 2017-09-29 | 成都深冷液化设备股份有限公司 | The composite bed adsorbent equipment of natural gas pretreatment |
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| CN104073310B (en) | 2018-04-13 |
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