CN109233927B - Recovery process of petroleum associated gas - Google Patents
Recovery process of petroleum associated gas Download PDFInfo
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- CN109233927B CN109233927B CN201811050779.2A CN201811050779A CN109233927B CN 109233927 B CN109233927 B CN 109233927B CN 201811050779 A CN201811050779 A CN 201811050779A CN 109233927 B CN109233927 B CN 109233927B
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- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
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- C10L3/101—Removal of contaminants
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
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Abstract
The invention discloses a recovery process of petroleum associated gas, which comprises the steps of primary impurity removal, deep impurity removal, filtration and dust removal, primary gas separation, re-separation of heavy components, recovery of light components, primary impurity removal, deep impurity removal and filtration and dust removal to purify the associated gas, wherein in the operation of primary gas separation, the associated gas is separated into the light components and the heavy components by utilizing the boiling point difference of each component in the associated gas through a pressurization and cooling mode, then light hydrocarbons such as methane, ethane and the like dissolved in the heavy components are removed, and the light components and the heavy components are separately recovered at normal temperature and normal pressure, so that the utilization added value of the associated gas is improved. The method has the characteristics of small investment, deep separation, high efficiency, low energy consumption and the like, can fully, efficiently and reasonably utilize the petroleum associated gas resources, adsorbs the impurity gas and the moisture in the associated gas by utilizing the composite molecular sieve layer in the recovery process, and has large adsorption capacity, high efficiency and good associated gas purification effect.
Description
Technical Field
The invention relates to the technical field of petroleum associated gas recovery, in particular to a recovery process of petroleum associated gas.
Background
Associated petroleum gas is a combustible mixture consisting of hydrocarbon gas mainly containing low-molecular saturated hydrocarbon and a small amount of non-hydrocarbon gas in subsurface porous stratum, and is a gaseous form of petroleum gas, most of the associated petroleum gas mainly contains methane, and contains hydrocarbons such as ethane, propane, butane, pentane and the like, and a small amount of gases such as nitrogen, carbon dioxide, hydrogen sulfide, helium, oxyhydrogen and the like. At present, the treatment mode of the oil associated gas generated in the process of oil field exploitation, particularly oil fields in small areas, is generally emptying, and the important problems brought by the method are air and soil pollution, increase of the danger of fire and explosion and waste of oil resources.
Foreign oil associated gas recovery technology began in the first light oil recovery plant established in 1904 in the united states. The foreign light hydrocarbon recovery method has advanced technology, and some countries have remarkable achievements in improving the processing depth, increasing the light hydrocarbon yield and reasonably utilizing the oil gas resources. Since the 70 s of the 20 th century, foreign light hydrocarbon recovery technology aims at saving energy, reducing consumption and improving light hydrocarbon yield, mainly adopts a low-temperature separation method, and develops towards the directions of small investment, deep separation, high efficiency, low energy consumption, skid-mounted installation, automation and the like.
China is a developing country, the full utilization and recovery of petroleum associated gas resources have important significance for the development of economy and society of China, and the national committee for development and improvement, the ministry of finance and the tax administration jointly issue a resource comprehensive utilization catalogue in 2003, clearly stipulate that 'light hydrocarbons are recovered and extracted in the production process of crude oil and natural gas' as a resource comprehensive utilization project, and give a certain tax preferential policy; at present, a plurality of large oil fields have purification and recovery technologies, but in a plurality of remote oil fields, due to the reasons of relatively complex terrain, difficulty in laying pipelines, poor economic benefit and the like, most of the produced petroleum associated gas is subjected to emptying combustion. Associated gas burnt or discharged in China is about 10 billion cubic meters, which is equivalent to 100 ten thousand tons of petroleum, and with the further development of inland oil fields, more and more petroleum associated gas resources are wasted, so that the oil field associated gas in remote areas needs to be recycled, and a proper purification and recovery method and a proper purification and recovery device for the petroleum associated gas need to be developed and designed.
The molecular sieve is a substance with uniform micropores and the pore diameter of the molecular sieve is equivalent to the size of general molecules, and the molecular sieve has a plurality of pore passages with uniform pore diameter and cavities with regular arrangement and large specific surface area in the structure. The micro holes have uniform diameter, strong polarity and coulomb field are arranged in the holes, strong adsorption capacity is shown for polar molecules (such as water) and unsaturated molecules, molecules smaller than the diameter of the pore channel can be adsorbed into the holes, and molecules larger than the pore channel are excluded, so that the molecules with different shapes and diameters, different polarity degrees, different boiling points and different saturation degrees can be separated, and the effect of screening the molecules is achieved. The common molecular sieve is mainly a zeolite molecular sieve synthesized by silicate and aluminate. Due to the unique porous structure, the molecular sieve can be applied to the fields of drying purification, adsorption separation, catalytic synthesis and the like, and is widely used in the industries of chemical industry, electronics, petrochemical industry, natural gas and the like.
Disclosure of Invention
In view of the above, the present invention provides a process for recovering associated gas, which improves the safety, energy saving performance, efficiency and practicability of the existing associated gas recovery method, and uses a composite molecular sieve layer to adsorb impurity gas and moisture in associated gas during the recovery process, and has the advantages of large adsorption capacity, high efficiency and good associated gas purification effect.
The invention solves the technical problems by the following technical means:
a process for recovering associated petroleum gas, comprising the steps of:
(1) preliminary impurity removal: collecting dispersed associated gas, separating the collected associated gas by using a separation tank, and removing part of water, micro solid particles and heavy hydrocarbon emulsion to obtain preliminarily impurity-removed associated gas;
(2) deep impurity removal: conveying the primarily-impurity-removed associated gas into a drying tower filled with a composite molecular sieve, and adsorbing residual moisture and impurity gas in the associated gas by using the composite molecular sieve;
the composite molecular sieve is of a double-layer shell-core structure, the shell layer is a metal organic framework for adsorbing impurity gas, and the core layer is a microporous zeolite molecular sieve for adsorbing moisture; the metal organic framework is formed by mutually connecting metal ions and PAMAM (polyamidoamine) dendrimer through self-assembly;
(3) filtering and dedusting: sending the associated gas from the drying tower into a dust filter, and filtering out composite molecular sieve dust entrained in the associated gas;
(4) primary gas separation: pressurizing the dust-filtered associated gas to 1.8-2.1Mpa, reducing the temperature of the pressurized associated gas to-40 to-60 ℃ through multi-stage cooling to obtain a gas-liquid mixture, and allowing the gas-liquid mixture to enter a low-temperature separator for gas-liquid separation to obtain a gaseous light component and a liquid heavy component;
(5) re-separation of heavy components: the separated heavy component enters a deethanizer to remove methane and ethane dissolved in the heavy component, and then is heated by a stabilizer to be changed into normal-temperature stable mixed hydrocarbon and put into a finished product tank;
(6) recovering light components: reducing the pressure of the separated light components to 0.1-0.2Mpa, heating to 23-25 ℃, and then sending into another finished product tank.
The purification of the associated gas is realized through the steps of preliminary impurity removal, deep impurity removal and filtering dust removal, in the operation of primary gas separation, the associated gas is divided into a light component and a heavy component by utilizing the boiling point difference of each component in the associated gas through a pressurizing and cooling mode, then light hydrocarbons such as methane, ethane and the like dissolved in the heavy component are removed, the light component and the heavy component are separately recovered under normal temperature and normal pressure, and the utilization added value of the associated gas is improved.
The existing technology for drying associated gas generally adopts a single-layer microporous zeolite molecular sieve to adsorb moisture in the associated gas, however, the outer surface of the microporous zeolite molecular sieve has more acid sites which are not limited by non-porous channels and have no shape-selective performance, and the existence of the acid sites enables the molecular sieve to easily form surface carbon deposit, block the porous channels and reduce the water absorption performance of the microporous zeolite molecular sieve. In addition, the microporous zeolite molecular sieve can adsorb other impurity gases such as H which can pass through the pore passages of associated gas while adsorbing moisture2S、CO2、CS2And COS and the like, thereby reducing the water capacity of the microporous zeolite molecular sieve and further reducing the water absorption performance of the microporous zeolite molecular sieve.
In the invention, in the process of deeply removing impurities from the associated gas, the composite molecular sieve layer is used for adsorbing impurity gas and moisture in the associated gas. The composite molecular sieve is of a double-layer shell-core structure, the outer shell layer is a metal organic framework for adsorbing impurity gas, the inner core layer is a microporous zeolite molecular sieve for adsorbing moisture, namely a layer of metal organic framework is wrapped outside the microporous zeolite molecular sieve, and the metal organic framework can realize shielding of acid sites on the outer surface of the microporous zeolite molecular sieve, so that carbon deposits on the surface of the microporous zeolite molecular sieve are prevented from blocking pore channels of the microporous zeolite molecular sieve, and the water absorption performance of the microporous zeolite molecular sieve is improved; the metal organic framework is formed by the mutual connection of metal ions and PAMAM (polyamidoamine) dendrimer through self assembly, the PAMAM is a polyamidoamine dendrimer with a highly branched network structure, and the surface of the PAMAM carries abundant amido and carboxyl groupsThe PAMAM has a highly branched network structure, and compared with a common metal organic framework, the metal organic framework synthesized by taking the PAMAM as the organic ligand has more micropores, more complex pore channels, larger specific surface area and stronger adsorption capacity. In addition, functional groups carried on the surface of the PAMAM have strong polarity, have strong adsorption effect on molecules with polarity, and can adsorb H existing in associated gas2S、CO2、CS2And impurity gases such as COS. Thus, the metal organic framework wrapped outside the microporous zeolitic molecular sieve may also be first aligned with H2S、CO2、CS2And the COS is adsorbed to prevent the COS from entering micropores of the microporous zeolite molecular sieve to be adsorbed so as to reduce the water capacity of the microporous zeolite molecular sieve, namely, a double-layer adsorption mode is adopted to carry out layered adsorption on impurity gas and moisture in the associated gas, so that the adsorption efficiency and the adsorption capacity are improved, and the purification effect of the associated gas is improved.
Further, the multi-stage cooling step in the step (4) is as follows: firstly, cooling pressurized associated gas to 30-40 ℃ through a condenser, then sequentially entering a shallow cooling heat exchanger and an ammonia evaporator to cool to-15 to-30 ℃, and finally cooling to-40 to-60 ℃ through a cryogenic heat exchanger.
Further, in the step (4), the light components include methane and ethane, and the heavy components include propane, butane and pentane.
Further, in the step (6), the pressure reduction and temperature increase operations of the light component are: the separated light components are primarily reduced to 0.9-1.0Mpa through a primary vortex tube, the light components after pressure reduction and a cryogenic heat exchanger are subjected to heat exchange to realize primary heating, the light components after primary heating enter a secondary vortex tube to be secondarily reduced to 0.1-0.2Mpa, the light components after secondary pressure reduction and the shallow heat exchanger are subjected to heat exchange, and the secondary heating is carried out to 23-25 ℃.
Further, the impurity gas includes H2S、CO2、CS2And COS.
Further, the preparation method of the composite molecular sieve comprises the following steps:
(1) dispersing microporous zeolite molecular sieve particles in 0.3-0.8 wt% of ammonium polyphosphate cationic solution, stirring for 30-100min, dispersing α -hopeite particles in 0.3-0.8 wt% of fatty alcohol acyl sodium sulfate solution, stirring for 40-120min, filtering, adding filtered α -hopeite particles into the ammonium polyphosphate cationic solution mixed with the microporous zeolite molecular sieve particles, stirring for 1-3h, standing for 30-60min, and filtering to obtain α -hopeite-microporous zeolite molecular sieve composite particles, wherein the weight ratio of the microporous zeolite molecular sieve to the α -hopeite is 1: 1-3;
(2) preparing a mixed solution of metal ions, PAMAM and ethanol, adding α -hopeite-microporous zeolite molecular sieve composite particles into the mixed solution, stirring at 30-50 ℃ for 6-12h, putting into a hydrothermal kettle for hydrothermal crystallization, washing a hydrothermal product to be neutral, and drying to obtain the composite molecular sieve, wherein the hydrothermal temperature is 180-250 ℃ and the hydrothermal time is 24-48 h.
In the invention, polyammonium cation is used for modifying the surface of a microporous zeolite molecular sieve to enable the microporous zeolite molecular sieve to have positive charges, α -hopeite is a seed crystal for promoting the growth of a metal organic framework, fatty alcohol sodium acyl sulfate is used as an anionic active agent to modify the surface of α -hopeite to enable α -hopeite to have negative charges, α -hopeite with negative charges is put into a polyammonium cation solution mixed with microporous zeolite molecular sieve particles, α -hopeite adsorbs the surfaces of the microporous zeolite molecular sieve to form hopeite-microporous zeolite molecular sieve composite particles under the action of the positive and negative charges, the prepared metal ion, PAMAM and ethanol mixed solution is used as a mother solution for synthesizing the metal organic framework, α -hopeite-microporous zeolite molecular sieve composite particles are added into the mother solution, α -hopeite is used as the seed crystal for promoting the growth of the metal organic framework, and finally the grown metal organic framework is coated on the surface of the microporous zeolite molecular sieve to form the composite molecular sieve.
Further, the metal ion is Mg2+、Al3+、Zn2+One or more of them.
Furthermore, the particle size of the microporous zeolite molecular sieve is 3-10mm, and the particle size of the α -hopeite particle is 5-20 nm.
Further, the microporous zeolite molecular sieve is an A-type zeolite molecular sieve.
Furthermore, the shell aperture of the composite molecular sieve is 0.4-1nm, and the specific surface area of the micropore is 500-2000m2The thickness is 0.5-2mm, and the pore diameter of the nuclear layer is 0.3-0.4 nm.
The invention has the beneficial effects that: compared with the existing oil-associated gas recovery method, the oil-associated gas recovery technology has the characteristics of small investment, deep separation, high efficiency, low energy consumption and the like, and can fully, efficiently and reasonably utilize oil-associated gas resources; the invention utilizes the double-layer composite molecular sieve which takes the metal organic framework as the shell and the microporous zeolite molecular sieve as the core to carry out layered adsorption on the impurity gas and the moisture in the associated gas, thereby improving the adsorption efficiency and the adsorption capacity of the molecular sieve and having good purification effect on the associated gas.
Drawings
FIG. 1 is a schematic flow diagram of a process for recovering associated petroleum gas in accordance with the present invention;
Detailed Description
The invention will be described in detail below with reference to the following figures and specific examples:
the first embodiment is as follows: preparing a composite molecular sieve by:
(1) dispersing 500g of 4A zeolite molecular sieve particles with the particle size of 3-6mm in 0.3 wt% of polyammonium cation solution under the action of ultrasound, stirring for 100min, dispersing 500g of α -hopeite particles with the particle size of 5-10nm in 0.3 wt% of fatty alcohol acyl sodium sulfate solution under the action of ultrasound, stirring for 120min, filtering, adding the filtered α -hopeite particles into the polyammonium cation solution mixed with the 4A zeolite molecular sieve particles, stirring for 2h, standing for 30min, and filtering to obtain α -hopeite-4A zeolite molecular sieve composite particles;
(2) weighing 100g of zinc acetate, 100g of PAMAM and 200ml of ethanol, adding into 800ml of water to prepare a mixed solution of zinc ions, PAMAM and ethanol, adding the α -hopeite-4A zeolite molecular sieve composite particles prepared in the step (1) into the mixed solution, stirring for 8 hours at the temperature of 40 ℃, putting into a hydrothermal kettle for hydrothermal crystallization, wherein the hydrothermal temperature is 180 ℃ and the hydrothermal time is 48 hours, washing a product after hydrothermal to be neutral, and drying to obtain the composite molecular sieve.
The prepared composite molecular sieve has a shell aperture of 0.4-0.7nm and a micropore specific surface area of 1000-2The thickness is 0.5mm, and the pore diameter of the nuclear layer is 0.35-0.4 nm.
Example two: preparing a second composite molecular sieve:
(1) dispersing 500g of 4A zeolite molecular sieve particles with the particle size of 5-10mm in 0.5 wt% of polyammonium cation solution under the action of ultrasound, stirring for 60min, dispersing 1000g of α -hopeite particles with the particle size of 10-15nm in 0.5 wt% of fatty alcohol acyl sodium sulfate solution under the action of ultrasound, stirring for 70min, filtering, adding the filtered α -hopeite particles into the polyammonium cation solution mixed with the 4A zeolite molecular sieve particles, stirring for 1h, standing for 45min, and filtering to obtain α -hopeite-4A zeolite molecular sieve composite particles;
(2) weighing 70g of aluminum nitrate, 100g of PAMAM and 200ml of ethanol, adding into 800ml of water to prepare a mixed solution of aluminum ions, PAMAM and ethanol, adding the α -hopeite-4A zeolite molecular sieve composite particles prepared in the step (1) into the mixed solution, stirring for 12 hours at the temperature of 30 ℃, putting into a hydrothermal kettle for hydrothermal crystallization, wherein the hydrothermal temperature is 250 ℃, the hydrothermal time is 24 hours, washing the product after hydrothermal to be neutral, and drying to obtain the composite molecular sieve.
The prepared composite molecular sieve has a shell aperture of 0.6-1nm and a micropore specific surface area of 500-1200m2G, thickness of 1.2mm, and pore diameter of 0.35-0.4 nm.
Example three: preparing the composite molecular sieve:
(1) dispersing 500g of 4A zeolite molecular sieve particles with the particle size of 4-8mm in 0.8 wt% of polyammonium cation solution under the action of ultrasound, stirring for 30min, dispersing 1500g of α -hopeite particles with the particle size of 12-20nm in 0.8 wt% of fatty alcohol acyl sodium sulfate solution under the action of ultrasound, stirring for 40min, filtering, adding the filtered α -hopeite particles into the polyammonium cation solution mixed with the 4A zeolite molecular sieve particles, stirring for 3h, standing for 60min, and filtering to obtain α -hopeite-4A zeolite molecular sieve composite particles;
(2) weighing 100g of magnesium carbonate, 100g of PAMAM and 200ml of ethanol, adding the weighed magnesium carbonate, 100g of PAMAM and 200ml of ethanol into 800ml of water to prepare a mixed solution of magnesium ions, PAMAM and ethanol, adding the α -hopeite-4A zeolite molecular sieve composite particles prepared in the step (1) into the mixed solution, stirring for 6 hours at the temperature of 50 ℃, putting the mixed solution into a hydrothermal kettle for hydrothermal crystallization, wherein the hydrothermal temperature is 200 ℃ and the hydrothermal time is 32 hours, washing a product after hydrothermal treatment to be neutral, and drying to obtain the composite molecular sieve.
The prepared composite molecular sieve has a shell aperture of 0.5-0.8nm and a micropore specific surface area of 1500-2The thickness is 2mm, and the pore diameter of the nuclear layer is 0.35-0.4 nm.
Example four: preparing the composite molecular sieve by the following steps:
(1) dispersing 500g of 3A zeolite molecular sieve particles with the particle size of 3-10mm in 0.5 wt% of polyammonium cation solution under the action of ultrasound, stirring for 60min, dispersing 800g of α -hopeite particles with the particle size of 5-20mm in 0.5 wt% of fatty alcohol acyl sodium sulfate solution under the action of ultrasound, stirring for 80min, filtering, adding the filtered α -hopeite particles into the polyammonium cation solution mixed with the 3A zeolite molecular sieve particles, stirring for 1.5h, standing for 50min, and filtering to obtain α -hopeite-3A zeolite molecular sieve composite particles;
(2) weighing 50g of zinc acetate, 50g of aluminum nitrate, 120g of PAMAM and 250ml of ethanol, adding the weighed materials into 1000ml of water to prepare a mixed solution of zinc ions, magnesium ions, PAMAM and ethanol, adding the α -hopeite-3A zeolite molecular sieve composite particles prepared in the step (1) into the mixed solution, stirring the mixed solution at the temperature of 30 ℃ for 12 hours, putting the mixed solution into a hydrothermal kettle for hydrothermal crystallization, wherein the hydrothermal temperature is 200 ℃ and the hydrothermal time is 32 hours, washing a product after hydrothermal treatment to be neutral, and drying the product to obtain the composite molecular sieve.
The prepared composite molecular sieve has the shell aperture of 0.4-1nm and the micropore specific surface area of 700-2000m2G, thickness of 1mm, and pore diameter of 0.3-0.35 nm.
Example five:
as shown in the attached figure 1, the recovery process of associated petroleum gas of the invention comprises the following steps:
(1) preliminary impurity removal: collecting dispersed associated gas, separating the collected associated gas by using a separation tank, and removing part of water, micro solid particles and heavy hydrocarbon emulsion to obtain preliminarily impurity-removed associated gas;
(2) deep impurity removal: sending the associated gas subjected to preliminary impurity removal into a drying tower filled with a composite molecular sieve, and adsorbing residual moisture and H in the associated gas by using the composite molecular sieve2S、CO2、CS2COS impurity gas; the composite molecular sieve is prepared in the first example, the second example, the third example or the fourth example;
(3) filtering and dedusting: sending the associated gas from the drying tower into a dust filter, and filtering out composite molecular sieve dust entrained in the associated gas;
(4) primary gas separation: pressurizing the dust-filtered associated gas to 1.8-2.1Mpa by using a supercharger, cooling the pressurized associated gas to 30-40 ℃ by using a condenser, sequentially entering a shallow cooling heat exchanger and an ammonia evaporator to cool to-15 to-30 ℃, finally cooling to-40 to-60 ℃ by using a cryogenic heat exchanger to obtain a gas-liquid mixture, and entering the gas-liquid mixture into a low-temperature separator to perform gas-liquid separation to obtain a gaseous light component and a liquid heavy component; the light components include methane and ethane and the heavy components include propane, butane and pentane.
(5) Re-separation of heavy components: the separated heavy component enters a deethanizer to remove methane and ethane dissolved in the heavy component, and then is heated by a stabilizer to be changed into normal-temperature stable mixed hydrocarbon and put into a finished product tank;
(6) recovering light components: the separated light component is primarily reduced to 0.9-1.0Mpa through a primary vortex tube, the light component after pressure reduction and a cryogenic heat exchanger are subjected to heat exchange to realize primary heating, the light component after primary heating enters a secondary vortex tube to be secondarily reduced to 0.1-0.2Mpa, the light component after secondary pressure reduction and the shallow cold heat exchanger are subjected to heat exchange, and the light component after secondary heating is sent into another finished product tank after secondary heating to 23-25 ℃.
Although the present invention has been described in detail with reference to the preferred embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the spirit and scope of the invention as defined in the appended claims. The techniques, shapes, and configurations not described in detail in the present invention are all known techniques.
Claims (9)
1. The process for recovering the petroleum associated gas is characterized by comprising the following steps of:
(1) preliminary impurity removal: collecting dispersed associated gas, separating the collected associated gas by using a separation tank, and removing part of water, micro solid particles and heavy hydrocarbon emulsion to obtain preliminarily impurity-removed associated gas;
(2) deep impurity removal: conveying the primarily-impurity-removed associated gas into a drying tower filled with a composite molecular sieve, and adsorbing residual moisture and impurity gas in the associated gas by using the composite molecular sieve; the composite molecular sieve is of a double-layer shell-core structure, the shell layer is a metal organic framework for adsorbing impurity gas, and the core layer is a microporous zeolite molecular sieve for adsorbing moisture; the metal organic framework is formed by mutually connecting metal ions and PAMAM (polyamidoamine) dendrimer through self-assembly;
(3) filtering and dedusting: sending the associated gas from the drying tower into a dust filter, and filtering out composite molecular sieve dust entrained in the associated gas;
(4) primary gas separation: pressurizing the dust-filtered associated gas to 1.8-2.1Mpa, reducing the temperature of the pressurized associated gas to-40 to-60 ℃ through multi-stage cooling to obtain a gas-liquid mixture, and allowing the gas-liquid mixture to enter a low-temperature separator for gas-liquid separation to obtain a gaseous light component and a liquid heavy component;
(5) re-separation of heavy components: the separated heavy component enters a deethanizer to remove methane and ethane dissolved in the heavy component, and then is heated by a stabilizer to be changed into normal-temperature stable mixed hydrocarbon and put into a finished product tank;
(6) recovering light components: reducing the pressure of the separated light components to 0.1-0.2Mpa, heating to 23-25 ℃, and sending into another finished product tank;
the preparation method of the composite molecular sieve comprises the following steps:
(1) dispersing microporous zeolite molecular sieve particles in 0.3-0.8 wt% of ammonium polyphosphate cationic solution, stirring for 30-100min, dispersing α -hopeite particles in 0.3-0.8 wt% of fatty alcohol acyl sodium sulfate solution, stirring for 40-120min, filtering, adding filtered α -hopeite particles into the ammonium polyphosphate cationic solution mixed with the microporous zeolite molecular sieve particles, stirring for 1-3h, standing for 30-60min, and filtering to obtain α -hopeite-microporous zeolite molecular sieve composite particles, wherein the weight ratio of the microporous zeolite molecular sieve to the α -hopeite is 1: 1-3;
(2) preparing a mixed solution of metal ions, PAMAM and ethanol, adding α -hopeite-microporous zeolite molecular sieve composite particles into the mixed solution, stirring at 30-50 ℃ for 6-12h, putting into a hydrothermal kettle for hydrothermal crystallization, washing a hydrothermal product to be neutral, and drying to obtain the composite molecular sieve, wherein the hydrothermal temperature is 180-250 ℃ and the hydrothermal time is 24-48 h.
2. The process for recovering associated petroleum gas according to claim 1, wherein the multi-stage temperature reduction step in the step (4) is: firstly, cooling pressurized associated gas to 30-40 ℃ through a condenser, then sequentially entering a shallow cooling heat exchanger and an ammonia evaporator to cool to-15 to-30 ℃, and finally cooling to-40 to-60 ℃ through a cryogenic heat exchanger.
3. The process for recovering associated petroleum gas as claimed in claim 2, wherein in the step (4), the light components comprise methane and ethane, and the heavy components comprise propane, butane and pentane.
4. A process for recovering associated petroleum gas according to claim 3, wherein in the step (6), the pressure reduction and temperature increase of the light components are carried out by: the separated light components are primarily reduced to 0.9-1.0Mpa through a primary vortex tube, the light components after pressure reduction and a cryogenic heat exchanger are subjected to heat exchange to realize primary heating, the light components after primary heating enter a secondary vortex tube to be secondarily reduced to 0.1-0.2Mpa, the light components after secondary pressure reduction and the shallow heat exchanger are subjected to heat exchange, and the secondary heating is carried out to 23-25 ℃.
5. The process of claim 1, wherein the impurity gas comprises H2S、CO2、CS2And COS.
6. The process of claim 5, wherein the metal ion is Mg2 +、Al3+、Zn2+One or more of them.
7. The process of claim 5, wherein the particle size of the microporous zeolite molecular sieve is 3-10mm, and the particle size of the α -hopeite is 5-20 nm.
8. The process of claim 7, wherein the microporous zeolite molecular sieve is a zeolite A molecular sieve.
9. The process as claimed in claim 5, wherein the composite molecular sieve has a shell pore size of 0.4-1nm and a micropore specific surface area of 500-2000m2The thickness is 0.5-2mm, and the pore diameter of the nuclear layer is 0.3-0.4 nm.
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