CN102527197A - Oil and gas decarburizing and desulfurizing process unit - Google Patents
Oil and gas decarburizing and desulfurizing process unit Download PDFInfo
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- CN102527197A CN102527197A CN2012100451543A CN201210045154A CN102527197A CN 102527197 A CN102527197 A CN 102527197A CN 2012100451543 A CN2012100451543 A CN 2012100451543A CN 201210045154 A CN201210045154 A CN 201210045154A CN 102527197 A CN102527197 A CN 102527197A
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Abstract
The invention provides an oil and gas decarburizing and desulfurizing process unit which comprises a compressed oil and gas storage tank, a carbon-sulfur gas storage tank, a hydrocarbon storage tank, a primary removal tower, a desorption tower and two refined removal towers, wherein ester absorbers, such as liquid carbonic acid acrylic ester, are stored in the primary removal tower and can absorb carbon-sulfur gas and water, the air pressure in the primary removal tower is 2-20 atmospheres, and the temperature is between 5DEG C and 20 DEG C; the air pressure in the desorption tower is 5-0.2 atmosphere; the refined removal towers contain granular absorbing materials, such as molecular sieve, which can be used for absorbing the carbon-sulfur gas and water, and the carbon-sulfur gas absorbed by the absorbing materials can be completely released to flow into the carbon-sulfur gas storage tank when the absorbing material isheated. The whole technological process or local process can operate under the control of an automatic control system. Two-level adsorption adopted in the unit can better remove the carbon-sulfur gas, water and solid wastes out of the oil and gas to obtain basically pure hydrocarbon gas. The whole unit is compact in line structure and is lower in use and maintenance costs and can be applied to small and medium-sized oil fields.
Description
Technical field
The present invention relates to the process unit that oil gas is transported to the preceding carbon dioxide removal of external pipe, depriving hydrogen sulphide, dehydration.
Background technology
Associated gas is the mist that is dissolved in the oil; Hydrocarbon content accounts for more than 50%, and the above component of C3 can reach 30%; Domestic oil field head space gas major part is through breather valve emptying, has both wasted resource, again contaminated environment.Natural gas, coalfield associated gas also have analogue.Among this paper above-mentioned three is referred to as oil gas.The direct discharging of oil gas is also more serious to the pollution of environment than freon, and they belong to non-renewable resources, and emptying causes the significant wastage of resource.Realize the recycling of petroleum resources, have important economic benefit and environmental benefit.But the carbon sulphur gas in the oil gas (this paper middle finger: carbon dioxide and hydrogen sulfide), moisture and hydro carbons (this paper middle finger: the organic molecule of carbon containing, hydrogen atom in the molecule) not easily separated.
The number of applying for a patent is 200610107366.4 " a kind of low-temp methanol washing process that is used for the natural gas _ raw material gas decarbonization, desulfuration "; Natural gas in low temperature methanol-eluted fractions carbon desulfurization process is a kind of a kind of technology that is exclusively used in natural gas _ raw material gas carbon dioxide removal, sulfide removal, and it is absorption tower, flash tank, heat exchanger, choke valve, stripper and the pipeline that is connected and detects the control instrument instrument and be formed by connecting.Contain part methyl alcohol in the carbon sulphur gas that this device is deviate from and wash raw material, the flow process of washing is shorter, and treatment effect is not good enough.And technological parameter such as temperature, pressure limits imprecision.
The number of applying for a patent is " reclaiming the composite decarbonizing solution of carbon dioxide in the mist " of 200710011329.8; This invention has designed a kind of novel composite decarbonizing solution, its by main absorbent components, help absorbent components, activating component, corrosion inhibiter, anti-oxidant and water to form.Wherein main absorbent components is AEE (AEEA), and helping absorbent components is AMP, MDEA and TEA, and activating component is MEA, DEA and PZ, and corrosion inhibiter is a sodium vanadate, and anti-oxidant is sodium sulfite and Schweinfurt green.The composite decarbonizing solution component is complicated, gives in the oil gas and brings new impurity, is unfavorable for that the further separation of hydro carbons is purified.
Mention the decarburization technique of propene carbonate (propylene carbonate acid esters) in " propene carbonate decarbonization process " literary composition in Ningxia petrochemical industry in February, 1999; But specifically do not introduce process data, its technological process is also unreasonable; Not mentionedly remove other low molecular effects, actual operability is not strong yet yet.And not having further smart separation of flow journey, treatment effect is not really desirable.
Summary of the invention
Goal of the invention: overcome the defective of the simple perhaps system complex of traditional oil gas decarbonization, desulfuration process unit, energy consumption height, poor effect, provide a kind of decarburization sulphur gas efficiency high, the decarbonization, desulfuration process unit that the THC rate of recovery is high.
Technical scheme: be to realize the object of the invention, a kind of oil gas decarbonization, desulfuration process unit that the present invention adopts contains compressed oil gas storage tank, carbon sulphur gas reservoir, hydro carbons storage tank, just takes off tower, desorber, two fine removing towers.
Just take off and have liquid carbon acid propylene acid esters in the tower (or methyl esters, ethyl ester, positive butyl ester, 2-Octyl Nitrite, ethyl acetate) and wait ester class absorbent, supply dissolving absorption carbon sulphur gas and moisture.The air pressure that just takes off in the tower is 2-20 atmospheric pressure; Just take off the attemperating unit that also contains absorbent in the tower, the temperature that can keep absorbent is the 5-20 degree, just takes off the bottom of tower and can leave useless admittedly sediment outlet; Sedimentation and filtration; The top of just taking off tower has outlet A to connect two fine removing towers respectively, and just taking off has outlet B in addition on the tower, supplies to have absorbed carbon sulphur gas and absorption of water agent inflow desorber.
Air pressure in the desorber is for being lower than 5 atmospheric pressure-0.2 atmospheric pressure, and the desorber top has outlet C to connect carbon sulphur gas reservoir, and outlet C can be connected with heat exchanger, and this heat exchanger can be connected the exchange cold with the attemperating unit that just takes off in the tower; In the desorber or contain water back, can help during heating the carbon sulphur gas that adsorbs in the absorbent is further discharged; Desorber outlet D arranged, the absorbent that supplies to have discharged carbon sulphur gas flows into through one-way cock and just takes off tower.
There is molecular sieve granular sorbing materials such as (or silica gel, active carbon, fluorite) in the fine removing tower, has the function of absorption carbon sulphur atmospheric carbon dioxide and water; Useless admittedly outlet can be left in the fine removing tower bottom, drops after the solid waste deposition in the fuel feeding gas.Fine removing tower is connected with outlet E, and the oil gas after the purification flows to the hydro carbons storage tank from outlet E; The fine removing tower top is connected with outlet F, and carbon sulphur gas discharges the back and flows to carbon sulphur gas reservoir from outlet F; Two fine removing tower effects are identical, use simultaneously, subsequent use or an absorption and a release function use in turn.
Fine removing tower can contain attemperating unit, and during cooling, hydro carbons partial liquefaction, carbon sulphur gas are adsorbed material absorption, are convenient to hydro carbons and separate with the carbon sulphur gas of gaseous state; During heating, can the carbon sulphur gas that adsorb in the sorbing material be discharged more up hill and dale.
Whole process flow or local flow process can be moved under the control of robot control system(RCS).
Carbon sulphur gas can pass through the defoaming device defoaming treatment earlier before getting into carbon sulphur gas reservoir, reclaims more smooth.
Ester class absorbent can be propylene carbonate acid methyl esters, propylene carbonate acetoacetic ester, the positive butyl ester of propylene carbonate acid, propylene carbonate acid 2-Octyl Nitrite or ethyl acetate.Outlet B can be connected with heat exchanger, and this heat exchanger is connected the exchange cold with the attemperating unit that just takes off in the tower.
Air pressure in the desorber is preferably negative pressure, contains water back in the desorber, can help during heating the carbon sulphur gas that adsorbs in the absorbent is further discharged;
The sorbing material of fine removing tower can be granular molecular sieve, silica gel, active carbon or fluorite.
Useless admittedly sediment outlet can be left in the bottom of just taking off tower, drops after the solid waste deposition in the fuel feeding gas in fine removing tower bottom or can also leave useless admittedly sediment outlet.
Carbon sulphur gas gets into before or after the carbon sulphur gas reservoir, can pass through the processing of removing carbon dioxide, and carbon dioxide reclaims or directly emptying separately.Hydrocarbon gas separated separately becomes low-carbon (LC) gas and high-carbon gas.
Beneficial effect:
Two-stage absorption of the present invention can separate carbon sulphur gas, moisture, the solid waste removed in the oil gas well, obtains the hydrocarbon gas of substantially pure.Regulate to ensure higher organic efficiency through rational design and automation, even gas component and tolerance fluctuation the time, the rate of recovery can guarantee also that more than 80% the hydro carbons overall recovery is near 100%, and wherein the above hydro carbons rate of recovery of C3 can reach 90%.
The pressure value of the temperature of liquid, gas is in moderate scope in all tank bodies, requires lower to temperature, the pressure of equipment; And absorbent and sorbing material are all reusable, and the construction and the use cost of equipment are lower.The entire equipment line construction is also relatively more succinct, and flow process is more clear, and equipment maintenance cost is lower.
And operational management is convenient; Gas recovery system for oil both can move 24 hours every days continuously; Also can periodic running; Can guarantee not have in two years the significant trouble operation, long perfomance life, the oil field, coalfield, oil gas field, the methane-generating pit that extensively are suitable for middle and small scale use as the primary treatment coordinative composition of equipments of oil gas.
Description of drawings
Accompanying drawing is the structural representation of the present invention when installing and using;
Among the figure, 1, the compressed oil gas storage tank; 2, just take off tower; 3, defoaming device; 4, hydro carbons pipeline; 5, carbon sulphur gas line; 6, carbon sulphur gas reservoir; 7, hydro carbons storage tank; 8, fine removing tower; 9, desorber; 10, useless admittedly sediment outlet; 11, one-way cock; 12 heat exchangers; 13, attemperating unit.
The specific embodiment
Below, in conjunction with accompanying drawing and embodiment the present invention is done explanation more specifically.
Embodiment
Device shown in accompanying drawing contains compressed oil gas storage tank 1, carbon sulphur gas reservoir 6, hydro carbons storage tank 7, just takes off tower 2, desorber 9, also contains two fine removing towers 8; Just take off and have liquid carbon acid acrylic acid methyl esters absorbent in the tower 2, the air pressure that just takes off in the tower 2 is 5-10 atmospheric pressure, just takes off the attemperating unit 13 that also contains absorbent in the tower 2, and keeping the temperature of absorbent is about the 5-10 degree; The top of just taking off tower 2 has outlet A to connect essence to take off 8 towers, and that just takes off tower 2 has outlet B in addition, supplies to have absorbed carbon sulphur gas and absorption of water agent inflow desorber 9.Air pressure in the desorber 9 is the atmospheric negative pressure of 0.8-0.3, and desorber 9 tops have outlet C to connect carbon sulphur gas reservoir 6, outlet C or be connected with heat exchanger 12, desorber 9 outlet D arranged in addition, the absorbent that supplies to have discharged carbon sulphur gas flows into and just takes off tower 2.
There is granular molecular sieve in the fine removing tower 8; Fine removing tower 8 is connected with outlet E, and the oil gas after the purification flows to hydro carbons storage tank 7 from outlet E; Fine removing tower 8 tops are connected with outlet F, and carbon sulphur gas discharges the back and flows to carbon sulphur gas reservoir 6 from outlet F; Two fine removing towers 8 adsorb and release function use in turn; Fine removing tower 8 contains attemperating unit, and during cooling, hydro carbons partial liquefaction, carbon sulphur gas are convenient to hydro carbons and are separated with the carbon sulphur gas of gaseous state by molecular sieve adsorption; During heating, can the carbon sulphur gas that adsorb in the molecular sieve be discharged more up hill and dale;
Useless admittedly sediment outlet 10 is left in fine removing tower 8 bottoms, drops after the solid waste deposition in the fuel feeding gas.
Whole process flow is moved under the control of robot control system(RCS).After this process processing, almost there are not carbon dioxide, hydrogen sulfide and steam in the oil gas, remaining clean hydro carbons oil gas.
Claims (7)
1. an oil gas decarbonization, desulfuration process unit contains compressed oil gas storage tank (1), carbon sulphur gas reservoir (6), hydro carbons storage tank (7), just takes off tower (2), desorber (9), it is characterized in that: also contain two fine removing towers (8);
Just take off and have liquid ester class absorbent in the tower (2), the air pressure that just takes off in the tower (2) is 2-20 atmospheric pressure, just takes off the attemperating unit (13) that also contains absorbent in the tower (2), and keeping the temperature of absorbent is the 5-20 degree; The top of just taking off tower (2) has outlet A to connect fine removing tower (8), and just taking off tower (2) has outlet B in addition, supplies to have absorbed carbon sulphur gas and absorption of water agent inflow desorber (9);
Air pressure in the desorber is the 5-0.2 atmospheric pressure; Desorber (9) top has outlet C to connect carbon sulphur gas reservoir (6); Export C or be connected with heat exchanger (12); In the desorber (9) or contain water back, desorber (9) outlet D arranged in addition, the absorbent that supplies to have discharged carbon sulphur gas flows into and just takes off tower (2);
Fine removing tower has granular sorbing material in (8); Fine removing tower (8) is connected with outlet E, and the oil gas after the purification flows to hydro carbons storage (7) from outlet E; Fine removing tower (8) top is connected with outlet F, and carbon sulphur gas discharges the back and flows to carbon sulphur gas reservoir (6) from outlet F; Two fine removing towers (8) effect is identical, use simultaneously, subsequent use or an absorption and a release function use in turn; Fine removing tower (8) or contain attemperating unit (13), during cooling, hydro carbons partial liquefaction, carbon sulphur gas are adsorbed material absorption, are convenient to hydro carbons and separate with the carbon sulphur gas of gaseous state; During heating, can the carbon sulphur gas that adsorb in the sorbing material be discharged more up hill and dale;
Whole process flow or local flow process are moved under the control of robot control system(RCS).
2. oil gas decarbonization, desulfuration process unit as claimed in claim 1 is characterized in that: ester class absorbent is propylene carbonate acid methyl esters, propylene carbonate acetoacetic ester, the positive butyl ester of propylene carbonate acid, propylene carbonate acid 2-Octyl Nitrite or ethyl acetate.
3. oil gas decarbonization, desulfuration process unit as claimed in claim 1 is characterized in that: outlet B is connected with heat exchanger (12), and this heat exchanger (12) is connected with attemperating unit (13) in just taking off tower (2) and exchanges cold.
4. oil gas decarbonization, desulfuration process unit as claimed in claim 1 is characterized in that: the air pressure in the desorber (9) is negative pressure, and desorber contains water back in (9), can help during heating the carbon sulphur gas that adsorbs in the absorbent is further discharged.
5. oil gas decarbonization, desulfuration process unit as claimed in claim 1 is characterized in that: the sorbing material of fine removing tower (8) is granular molecular sieve, silica gel, active carbon or fluorite.
6. oil gas decarbonization, desulfuration process unit as claimed in claim 1; It is characterized in that: useless sediment outlet (10) is admittedly left in the bottom of just taking off tower (2); Drop after the solid waste deposition in the fuel feeding gas in fine removing tower bottom or also leave useless sediment outlet (10) admittedly.
7. like claim 1 or 4 described oil gas decarbonization, desulfuration process units, it is characterized in that: carbon sulphur gas gets into before or after the carbon sulphur gas reservoir (6), through removing the processing of carbon dioxide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2012100451543A CN102527197A (en) | 2012-02-27 | 2012-02-27 | Oil and gas decarburizing and desulfurizing process unit |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012100451543A CN102527197A (en) | 2012-02-27 | 2012-02-27 | Oil and gas decarburizing and desulfurizing process unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108939809A (en) * | 2018-07-20 | 2018-12-07 | 北京欧美中科学技术研究院 | A kind of oil gas decarbonization, desulfuration process unit |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1334313A (en) * | 2000-07-13 | 2002-02-06 | 张国瑞 | Adsorption-absorption process for recovering oil gas |
| CN1546206A (en) * | 2003-12-09 | 2004-11-17 | 南化集团研究院 | Method for removing sulfides and carbon dioxide by high pressure |
| CN101016492A (en) * | 2006-10-30 | 2007-08-15 | 河南中原绿能高科有限责任公司 | Low-temperature methanol washing process for decarbonization and desulfurization of natural gas feed gas |
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2012
- 2012-02-27 CN CN2012100451543A patent/CN102527197A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1334313A (en) * | 2000-07-13 | 2002-02-06 | 张国瑞 | Adsorption-absorption process for recovering oil gas |
| CN1546206A (en) * | 2003-12-09 | 2004-11-17 | 南化集团研究院 | Method for removing sulfides and carbon dioxide by high pressure |
| CN101016492A (en) * | 2006-10-30 | 2007-08-15 | 河南中原绿能高科有限责任公司 | Low-temperature methanol washing process for decarbonization and desulfurization of natural gas feed gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108939809A (en) * | 2018-07-20 | 2018-12-07 | 北京欧美中科学技术研究院 | A kind of oil gas decarbonization, desulfuration process unit |
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Application publication date: 20120704 |