CN114797266B - Ethylene glycol regeneration treatment system based on micron filtration - Google Patents
Ethylene glycol regeneration treatment system based on micron filtration Download PDFInfo
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- CN114797266B CN114797266B CN202210556685.2A CN202210556685A CN114797266B CN 114797266 B CN114797266 B CN 114797266B CN 202210556685 A CN202210556685 A CN 202210556685A CN 114797266 B CN114797266 B CN 114797266B
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 201
- 238000001914 filtration Methods 0.000 title claims abstract description 68
- 238000011069 regeneration method Methods 0.000 title claims abstract description 23
- 230000008929 regeneration Effects 0.000 title claims abstract description 22
- 238000001179 sorption measurement Methods 0.000 claims abstract description 49
- 239000002245 particle Substances 0.000 claims abstract description 40
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 37
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 34
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 150000003839 salts Chemical class 0.000 claims abstract description 17
- 239000013078 crystal Substances 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 34
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 28
- 239000003345 natural gas Substances 0.000 claims description 14
- 238000001471 micro-filtration Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 claims description 5
- 229910052740 iodine Inorganic materials 0.000 claims description 5
- 239000011630 iodine Substances 0.000 claims description 5
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- -1 salt ions Chemical class 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 238000011033 desalting Methods 0.000 claims description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims 1
- 239000011780 sodium chloride Substances 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 47
- 231100000719 pollutant Toxicity 0.000 abstract description 47
- 230000003749 cleanliness Effects 0.000 abstract description 13
- 239000011882 ultra-fine particle Substances 0.000 abstract description 8
- 239000007787 solid Substances 0.000 abstract description 4
- 239000000356 contaminant Substances 0.000 description 23
- 238000000034 method Methods 0.000 description 21
- 230000008569 process Effects 0.000 description 20
- 239000000243 solution Substances 0.000 description 18
- 238000004088 simulation Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000011109 contamination Methods 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 5
- 238000010612 desalination reaction Methods 0.000 description 5
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000013618 particulate matter Substances 0.000 description 5
- 238000005260 corrosion Methods 0.000 description 4
- 230000001052 transient effect Effects 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000013178 mathematical model Methods 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 101100459773 Caenorhabditis elegans nas-11 gene Proteins 0.000 description 2
- 101100459776 Caenorhabditis elegans nas-14 gene Proteins 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012527 feed solution Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000009545 invasion Effects 0.000 description 2
- 239000010687 lubricating oil Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000000087 stabilizing effect Effects 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- 206010033799 Paralysis Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000006900 dealkylation reaction Methods 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- 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
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2023—Glycols, diols or their derivatives
Abstract
The invention relates to a glycol regeneration treatment system based on micron filtration, which comprises a pretreatment unit, a micron filtration adsorption unit, a depth treatment unit and a micron filtration unit which are connected in sequence; the invention can effectively eliminate the accumulated pollution of ultrafine particle pollutants (especially solid particles of 1-5 mu m) and hydrocarbon pollutants, ensures the system to operate under the target cleanliness, and improves the effectiveness, stability and economy of the system operation; and the micron filter unit arranged at the downstream of the advanced treatment unit effectively filters monovalent salt crystal particles in the ethylene glycol lean solution, improves the filtering efficiency of the low-valent salt crystal particles, prevents the accumulated pollution of the low-valent salt, and prolongs the operation period of the system.
Description
Technical Field
The invention relates to the technical field of natural gas exploitation and natural gas purification, in particular to a glycol regeneration treatment system based on micron filtration.
Background
In the development process of a deep water gas well, natural gas extracted from a wellhead is generally high in water content, hydrate formation is extremely easy to induce, and the natural gas is continuously gathered in pipelines and equipment to cause local blockage and even paralysis of the whole system, so that an alcohol injection process is required to be set, and ethylene glycol (MEG) is used as an inhibitor to be injected into an underground production process system so as to reduce the generation of the hydrate. The alcohol injection process has important significance for safe and efficient exploitation of deep water natural gas.
In the process of alcohol injection, the consumption of the ethylene glycol is large (natural gas is injected in proportion) and the price is high, so that the used ethylene glycol is required to be regenerated and recycled, thereby greatly reducing the consumption of the ethylene glycol and effectively reducing the production operation cost. The glycol recovery and regeneration treatment system (MRU system for short) is used for receiving the glycol rich liquid from the underwater natural gas exploitation process system, carrying out regeneration treatment on the glycol rich liquid to obtain the glycol lean liquid with qualified technical indexes, and conveying the glycol lean liquid back to the wellhead injection point for recycling. MRU systems are key technical equipment for deep water natural gas production.
Glycol rich solutions from production process systems contain a large number of poorly soluble contaminants (solid particles, heavy hydrocarbons, organic degradation products) and soluble contaminants (water, light hydrocarbons, low-cost salts, etc.), the presence of which can cause problems of bubbling, fouling, plugging, etc. of MRU systems and of the injection process systems. Because the ethylene glycol is recycled, along with the extension of the operation time, the pollutants can generate an accumulation effect, so that the pollutants of the system are rapidly increased, the working efficiency and the operation cost of the system are affected, and the system is also failed and stopped when serious, therefore, a filtration and purification unit is usually arranged in the MRU system, and the insoluble pollutants are effectively removed in time, so that the pollution degree is kept within an allowable range. However, the existing MRU system cannot effectively filter out particle pollutants (especially particles with the particle diameters of less than 10 mu m, particularly particles with the particle diameters of 1-5 mu m) and hydrocarbon pollutants thereof, so that ultrafine particle pollutants (particles with the particle diameters of 1-5 mu m) are accumulated, and the accumulated pollution of the ultrafine particle pollutants can promote the formation of oil sludge (semisolid and viscous pollutants), thereby causing the problems of scaling, blocking and the like of the system, affecting the working performance of the system, and causing system faults and even shutdown.
Disclosure of Invention
The invention aims to provide a glycol regeneration treatment system based on micron filtration, which solves the problems in the background technology.
In order to solve the technical problems, the technical scheme provided by the invention is as follows:
a glycol regeneration treatment system based on micron filtration comprises a pretreatment unit, a micron filtration adsorption unit, a depth treatment unit and a micron filtration unit which are connected in sequence;
the pretreatment unit is used for treating the ethylene glycol rich liquid conveyed into the pretreatment unit, the ethylene glycol feed liquid treated by the pretreatment unit is conveyed to the micron filtration adsorption unit for treatment, the ethylene glycol feed liquid treated by the micron filtration adsorption unit is conveyed to the advanced treatment unit for treatment, the ethylene glycol lean liquid treated by the advanced treatment unit is conveyed to the micron filtration unit for filtration, and the ethylene glycol lean liquid treated by the micron filtration unit can be conveyed to the natural gas exploitation system for cyclic utilization.
As a preferred embodiment, the microfiltration adsorption unit comprises a first microfiltration and an activated carbon adsorber.
As a preferable scheme, the first micron filter is arranged between the pretreatment unit and the activated carbon adsorber, the glycol feed liquid treated by the pretreatment unit is conveyed to the first micron filter for filtering treatment, the glycol feed liquid treated by the first micron filter is conveyed to the activated carbon adsorber for adsorption treatment, and the glycol feed liquid treated by the activated carbon is conveyed to the advanced treatment unit for treatment.
As a preferred embodiment, the micro filter unit comprises a second micro filter.
As a preferable scheme, the adsorption efficiency of the activated carbon adsorber is more than 80%, and the iodine adsorption value is more than 1200mg/g.
As a preferable scheme, the filtering precision of the first micron filter and the second micron filter is 1 mu m, and the fouling capacity of the micron filters is more than or equal to 650 g/(L/min).
As a preferred embodiment, the filter elements of the first and second micrometer filters are folded filter elements.
As a preferred scheme, the adsorption efficiency of the activated carbon adsorber is more than 80 percent, and the iodine adsorption value is more than 1200mg/g.
The invention has the advantages that:
the invention can effectively eliminate the accumulated pollution of ultrafine particle pollutants (solid particles of 1-5 mu m) and hydrocarbon pollutants, ensure the system to operate under the target cleanliness, and improve the effectiveness, stability and economy of the system operation; and the micron filter unit arranged at the downstream of the advanced treatment unit effectively filters monovalent salt crystal particles in the ethylene glycol lean solution, improves the filtering efficiency of the low-valent salt crystal particles, prevents the accumulated pollution of the low-valent salt, and prolongs the operation period of the system.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a process flow diagram of the present invention.
FIG. 2 is a schematic diagram of a conventional system process flow in example 2.
FIG. 3 is a graph showing the simulation of the variation with time of the particulate contaminants of three particle sizes (1 μm, 5 μm, 10 μm) using a filter having a filtration accuracy of 10 μm in example 2.
FIG. 4 is a graph showing the simulation of the variation with time of the particulate contaminants of three particle sizes (1 μm, 5 μm, 10 μm) using a 1 μm filter in example 2.
FIG. 5 is a flow chart of control of liquid hydrocarbon contaminants in the MRU system of example 2, FIG. 5a is a MRU system without an adsorption unit, and FIG. 5b is a simulated MRU system with an adsorption unit according to the present invention.
FIG. 6 is a simulated plot of the amount of hydrocarbon contaminants in the MRU system over time for example 2 at different adsorption efficiencies.
FIG. 7 is a simulated plot of hydrocarbon contaminant levels in an MRU system (with adsorption units) over time without the adsorption units in example 2.
Description of the embodiments
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1: a glycol regeneration treatment system based on micron filtration comprises a pretreatment unit, a micron filtration adsorption unit, a depth treatment unit and a micron filtration unit which are connected in sequence;
as shown in fig. 1, the pretreatment unit is used for treating the ethylene glycol rich solution conveyed into the pretreatment unit, the ethylene glycol feed solution treated by the pretreatment unit is conveyed to the micron filtration adsorption unit for treatment, the ethylene glycol feed solution treated by the micron filtration adsorption unit is conveyed to the advanced treatment unit for treatment, the ethylene glycol lean solution treated by the advanced treatment unit is conveyed to the micron filtration unit for filtration, and the ethylene glycol lean solution treated by the micron filtration unit can be conveyed to the natural gas exploitation system for cyclic utilization.
The ethylene glycol rich liquid in this embodiment may be derived from an MEG tank of the ethylene glycol rich solution, or the pretreatment unit is connected to a three-phase separator in the natural gas extraction system, that is, the ethylene glycol liquid material (the ethylene glycol rich liquid) obtained after separation by the three-phase separator is conveyed to the pretreatment unit for treatment.
The pretreatment unit in the invention comprises a pretreatment device for removing light hydrocarbon and divalent salt ions in the ethylene glycol rich liquid, which is a conventional technology in the field, for example, a three-phase separator can be adopted for flash evaporation to remove the light hydrocarbon, or a medicament is adopted for precipitation to separate out the divalent salt ions, and the details are not repeated here.
The advanced treatment unit comprises a dehydration regeneration device for removing water in the ethylene glycol rich liquid and a desalting device for removing monovalent salt in the salt-containing ethylene glycol lean liquid, wherein the advanced treatment unit is used for treating the water and the monovalent salt in the ethylene glycol rich liquid, is a conventional technology in the field, is not described in detail herein, and can adopt an evaporative crystallization and rectification device; the ethylene glycol lean solution obtained after the treatment of the advanced treatment unit generally contains a large amount of monovalent salt crystal particles, and if the ethylene glycol lean solution is directly conveyed back to the natural gas exploitation system without the treatment, accumulated pollution in the MRU system can be caused, pipelines and equipment are easy to corrode, scaling and blocking are easy to occur, and the operation period of the system is influenced.
The micron filtration adsorption unit comprises a first micron filter and an activated carbon adsorber.
The first micron filter is arranged between the pretreatment unit and the activated carbon absorber, the glycol feed liquid treated by the pretreatment unit is conveyed into the first micron filter for filtering treatment, the glycol feed liquid treated by the first micron filter is conveyed into the activated carbon absorber for adsorption treatment, and the glycol feed liquid treated by the activated carbon is conveyed into the advanced treatment unit for treatment.
The micron filtration adsorption unit can effectively remove the particle pollutants and heavy hydrocarbons contained in the glycol feed liquid after being treated by the pretreatment unit.
The micron filtration unit includes a second micron filter.
The adsorption efficiency of the activated carbon adsorber is more than 80%, and the iodine adsorption value is more than 1200mg/g.
The filtering precision of the first micron filter and the second micron filter is 1 mu m, and the dirt holding capacity of the micron filters is more than or equal to 650 g/(L/min).
The filter elements of the first micron filter and the second micron filter adopt folding filter elements.
The cartridges of the first and second micron filters in this embodiment may be bulk sandwich-type cartridges.
The adsorption efficiency of the activated carbon adsorber is more than 80%, and the iodine adsorption value is more than 1200mg/g.
Example 2: in the embodiment, the control effect of the particulate pollutants and the hydrocarbon pollutants is simulated by adopting the mathematical model of the regeneration treatment system.
As shown in fig. 2, in the conventional system in the prior art, a filtering and purifying unit is only arranged between a pretreatment unit and a deep treatment unit, the filtering and purifying unit comprises a filter and an adsorber, and the filtering and purifying unit of the filter has a filtering precision of 10 μm or more, and proved by production experience, although the filtering and purifying unit can effectively remove particle pollutants with the particle size of 10 μm or more, the particle pollutants with the particle size of 10 μm or less (especially particles with the particle size of 1-5 μm) cannot be effectively filtered, the adsorption efficiency of hydrocarbon pollutants is less than 60%, the accumulated pollution of ultrafine particle pollutants (particles with the particle size of 1-5 μm) and hydrocarbon pollutants can be caused, and the accumulated pollution of ultrafine particle pollutants and hydrocarbon pollutants can promote the formation of fatlute (semisolid and viscous pollutants), thereby causing problems such as scaling and blockage of the system, affecting the working performance of the system, and causing system faults and even shutdown.
The conventional system and the regeneration system of the invention in the embodiment all convey the ethylene glycol lean solution after the advanced treatment unit to the natural gas exploitation system for recycling, and the system pollution balance (target cleanliness control) of the MRU system can be a complex dynamic process, so that on one hand, the pollutants in the system are continuously increased due to continuous generation of the pollutants, including moisture ingress, reaction generation, corrosion generation, filtration medium shedding, organic matter degradation and the like, and on the other hand, the pollutants are removed through the filtration unit and the adsorption unit. When the system generation and the rejection are equal, the system pollution reaches dynamic balance.
The preconditions for numerical modeling of the particulate contamination control simulation of the two systems of this embodiment are:
the mathematical model is built on the assumption that: (1) uniform distribution of contaminants; (2) Other accessories in the system except the filter do not retain pollutants; (3) relatively stable pollutant formation rate; (4) the filtration ratio of the filter is relatively stable; and (5) stabilizing the flow of the system.
In this embodiment, it is assumed that the basic process parameters of the MRU system are:
total volume of glycol solution in system: 30m 3 ；
Circulation working flow rate: 5m 3 /h；
Ethylene glycol rich liquor pollution degree: NAS14 (ISO 25/23/20);
ethylene glycol lean solution pollution degree: NAS11 (ISO 22/20/17);
target cleanliness control requirements: particles of > 1 μm 320000/mL;
particles 80000/mL > 5 μm;
10000/mL of particles of > 10 μm.
Taking a two-channel filter unit as an example according to a system pollutant balance control chart, the instantaneous particle pollution degree in the glycol desalination and regeneration system can be obtained within any father time, and the instantaneous particle pollution degree is as follows:
（1）
wherein C is n Representing the concentration of transient particulate matter at equilibrium, the value of which is determined according to the target cleanliness, this example requires a pollution level of NAS11 (ISO 22/20/17);
C n-1 -the transient particulate matter concentration at the previous iteration of the equilibrium is reached;
R 1 -absorbing the intrusion;
R 2 -reaction to form-absorber;
R 3 -reacting to form a-dealkylation unit;
R 4 -a reaction to form-a divalent salt removal unit;
R 5 -reaction to form-filtration media shedding;
R 6 -a reaction generation-regeneration unit;
R 7 -corrosion formation;
β 1 -the filtration ratio of the filtration unit 1;
β 2 -the filtration ratio of the filtration unit 2;
q-system circulation flow;
v-total volume of ethylene glycol solution;
t—cyclic process time step.
The above steps are transformed and arranged to obtain:
（2）
when t tends to infinity, the differential equation can be derived:
（3）
solving to obtain:
（4）
wherein C is 0 Represents the transient particulate matter concentration of the initial ethylene glycol rich solution, and is rated NAS14 (ISO 24/23/20).
Equation (4) expresses the relationship between the steady state value of the contamination level and the filter filtration ratio, the contamination generation rate, and the system flow rate. When the system starts to work with a certain initial pollution degree, under the action of circulation flow, the system continuously generates pollutant to be immersed in the working process, meanwhile, the filter continuously eliminates pollution, on the premise that the filtering precision of the filter is qualified, the pollution degree of the system can be monotonically decreased along with the increase of time, and finally, the target pollution degree of the system is reached after circulation for a certain times.
Aiming at the pollution control process of the glycol desalination regeneration system, a computer is utilized to run a simulation model, simulate the running state of an actual system and the process of the change of the actual system along with time, and obtain the simulation output parameters and the basic characteristics of the simulated system through the observation and statistics of the simulation running process, so as to estimate and infer the real parameters and the real performances of the actual system. A step of
This example shows that when the filtration accuracy of the filter is 10 μm and the number of > 1 μm and > 5 μm particle contaminants is rapidly increased over time, as shown in fig. 3 and 4, the cumulative contamination of > 1 μm and > 5 μm particle contaminants cannot be eliminated by the filter with filtration accuracy of 10 μm, and the simulation calculation data shows that the achievement and maintenance of the target cleanliness of > 1 μm and > 5 μm particles in the system cannot be ensured by the conventional MRU system using the 10 μm filter, as shown in fig. 3 and 4. As can be seen from FIG. 4, when the filtration accuracy is 1 μm, all of the particle contaminants of > 1 μm, > 5 μm and > 10 μm can reach the target cleanliness, which means that the filter with the filtration accuracy of 1 μm can effectively eliminate the accumulated contamination of the ultrafine particle contaminants, so that the system can operate within the allowable target cleanliness range (the particle number of > 1 μm is 30000/ml, the particle number of > 5 μm is 7500/ml and the particle number of > 10 μm is 1000/ml).
The liquid hydrocarbon pollutant and the particle pollutant in the MRU system are subjected to a complex dynamic process, the system is simulated to be subjected to single-loop analysis, the single-loop analysis comprises an immersion link (contact invasion of original lubricating oil and reaction generation after organic matter degradation) of the liquid hydrocarbon pollutant, and an adsorption control unit of the liquid hydrocarbon pollutant is not provided with an adsorption unit, and a liquid hydrocarbon pollutant control flow chart in the MRU system provided with the adsorption unit is shown in fig. 5a and 5b.
The mathematical model is built on the assumption that: (1) uniform distribution of contaminants; (2) Other accessories in the system except the filter do not retain pollutants; (3) relatively stable pollutant formation rate; (4) the filtration ratio of the filter is relatively stable; and (5) stabilizing the flow of the system.
According to the system pollutant balance control diagram, in any father time, the instantaneous hydrocarbon pollutant pollution degree in the glycol desalination regeneration system can be obtained as follows:
（5）
wherein: cn—transient hydrocarbon contaminant concentration at equilibrium, the value of which is determined based on target cleanliness;
cn-1-the hydrocarbon contaminant concentration at the previous iteration of the equilibrium is reached;
t1-contact invasion of lubricating oil;
t2-organic matter is generated by reaction after degradation;
β1—adsorption ratio of adsorption units;
q-system circulation flow;
v-total volume of ethylene glycol solution;
t—cyclic process time step.
The above steps are transformed and arranged to obtain:
（6）
when t tends to infinity, the differential equation can be derived:
（7）
solving to obtain:
（8）
wherein: c0 -initial transient hydrocarbon contaminant concentration of the ethylene glycol rich solution;
equation (8) expresses the relationship between the steady state value of the contamination level and the adsorber adsorption ratio, the contamination generation rate, and the system flow rate. When the system starts to work with a certain initial pollution degree, under the action of circulating flow, the system continuously generates pollutant to be immersed in the working process, and meanwhile, the absorber continuously eliminates pollution, on the premise that the absorption precision of the absorber is qualified, the pollution degree of the system can be monotonically decreased along with the increase of time, and finally, the target pollution degree of the system is reached after the circulation is performed for a certain number of times.
Aiming at the pollution control process of the glycol desalination regeneration system, a computer is utilized to run a simulation model, simulate the running state of an actual system and the process of the change of the actual system along with time, and obtain the simulation output parameters and the basic characteristics of the simulated system through the observation and statistics of the simulation running process, so as to estimate and infer the real parameters and the real performances of the actual system.
The simulation results are shown in fig. 6 and 7, and as can be seen from fig. 6, the system with the adsorption unit can effectively reduce the quality of hydrocarbon pollutants; at adsorption efficiencies of 50% and 60%, hydrocarbon contaminants in the system have not been able to be effectively controlled; when the adsorption efficiency is 70% -90%, the increase of the hydrocarbon pollutant amount with time is in a decreasing trend, and along with the improvement of the adsorption efficiency, the time required for the hydrocarbon pollutant to reach the target cleanliness is shortened, so that the control of the hydrocarbon pollutant is more efficient. When the adsorption efficiencies were 70%, 80%, 90%, respectively, the times for the hydrocarbon contaminants to reach the target cleanliness were 21.5 hours, 13.4 hours, 10.8 hours. It can be seen from fig. 7 that without the adsorption unit, the increase in the amount of hydrocarbon contaminants in the system over time is an exponential increase, and if hydrocarbon contaminants are not controlled, small molecular hydrocarbon contaminants accumulate and bind, resulting in plugging and corrosion of pipelines and equipment.
From example 2, it is seen that (1) without the adsorption unit, the liquid hydrocarbon contaminant quality increases exponentially, and small molecular hydrocarbon contaminants accumulate and bind, resulting in clogging and corrosion of pipelines and equipment. (2) The adsorption unit is added, so that the quality of hydrocarbon pollutants can be effectively reduced; and along with the improvement of adsorption efficiency, the time required for reaching the target cleanliness is shortened, and the method has a key meaning for maintaining the operation stability and reliability of the glycol desalination recovery system.
Therefore, the regeneration treatment system can effectively eliminate the accumulated pollution of ultrafine particle pollutants (solid particles of 1-5 mu m) and hydrocarbon pollutants, ensure the system to operate under the target cleanliness, and improve the effectiveness, stability and economy of the system operation; and by arranging the micron filtration unit at the downstream of the advanced treatment unit, the filtration efficiency of low-valence salt crystallization particles can be improved, the accumulated pollution of low-valence salt is prevented, and the operation period of the system is ensured.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (4)
1. The glycol regeneration treatment system based on micron filtration is characterized by comprising a pretreatment unit, a micron filtration adsorption unit, a depth treatment unit and a micron filtration unit which are connected in sequence;
the pretreatment unit is used for treating the ethylene glycol rich liquid conveyed into the pretreatment unit, the ethylene glycol feed liquid treated by the pretreatment unit is conveyed to the micron filtration adsorption unit for treatment, the ethylene glycol feed liquid treated by the micron filtration adsorption unit is conveyed to the advanced treatment unit for treatment, the ethylene glycol lean liquid treated by the advanced treatment unit is conveyed to the micron filtration unit for filtration, and the ethylene glycol lean liquid treated by the micron filtration unit is conveyed to the natural gas exploitation system for cyclic utilization;
the micron filter unit arranged at the downstream of the advanced treatment unit filters monovalent salt crystal particles in the ethylene glycol lean solution;
the pretreatment unit comprises a pretreatment device which is responsible for removing light hydrocarbon and bivalent salt ions in the ethylene glycol rich liquid;
the advanced treatment unit comprises a dehydration regeneration device for removing water in the ethylene glycol rich liquid and a desalting device for removing monovalent salt in the saline ethylene glycol lean liquid, and is used for treating the water and monovalent salt in the ethylene glycol rich liquid;
the micron filtration and adsorption unit comprises a first micron filter and an activated carbon adsorber;
the micron filtration unit comprises a second micron filter;
the filtering precision of the first micron filter and the second micron filter is 1 mu m, and the dirt holding capacity of the micron filters is more than or equal to 650 g/(L/min).
2. The glycol regeneration treatment system based on micro-filtration according to claim 1, wherein the first micro-filtration is arranged between the pretreatment unit and the activated carbon adsorber, the glycol feed liquid treated by the pretreatment unit is conveyed to the first micro-filtration for filtration treatment, the glycol feed liquid treated by the first micro-filtration is conveyed to the activated carbon adsorber for adsorption treatment, and the glycol feed liquid treated by the activated carbon is conveyed to the advanced treatment unit for treatment.
3. A microfiltration based glycol regeneration treatment system according to claim 1 wherein the cartridges of the first and second microfiltration devices are pleated cartridges.
4. A microfiltration based ethylene glycol regeneration treatment system according to claim 1, wherein the activated carbon adsorber has an adsorption efficiency of > 80% and an iodine adsorption value of > 1200mg/g.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104707352A (en) * | 2015-03-30 | 2015-06-17 | 中海石油(中国)有限公司 | Desalting regeneration device of salt-containing ethylene glycol solution |
| CN107349971A (en) * | 2017-08-09 | 2017-11-17 | 西南石油大学 | A kind of ethylene glycol rich solution desalinating process and device |
| WO2018115442A1 (en) * | 2016-12-23 | 2018-06-28 | Nov Process & Flow Technologies As | Hydrate inhibitor recovery system |
| CN209740902U (en) * | 2019-04-01 | 2019-12-06 | 安洁行方流体管理技术有限公司 | Oily waste liquid treatment system of machinery trade |
| CN112121452A (en) * | 2020-09-27 | 2020-12-25 | 江苏科技大学 | Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation |
| CN112274958A (en) * | 2020-09-28 | 2021-01-29 | 重庆前卫科技集团有限公司 | Ethylene glycol regeneration and recovery system and ethylene glycol recovery method in deep sea natural gas development process |
| CN213885035U (en) * | 2020-09-28 | 2021-08-06 | 重庆前卫科技集团有限公司 | Ethylene glycol regeneration and recovery system in deep sea natural gas development process |
-
2022
- 2022-05-20 CN CN202210556685.2A patent/CN114797266B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104707352A (en) * | 2015-03-30 | 2015-06-17 | 中海石油(中国)有限公司 | Desalting regeneration device of salt-containing ethylene glycol solution |
| WO2018115442A1 (en) * | 2016-12-23 | 2018-06-28 | Nov Process & Flow Technologies As | Hydrate inhibitor recovery system |
| CN107349971A (en) * | 2017-08-09 | 2017-11-17 | 西南石油大学 | A kind of ethylene glycol rich solution desalinating process and device |
| CN209740902U (en) * | 2019-04-01 | 2019-12-06 | 安洁行方流体管理技术有限公司 | Oily waste liquid treatment system of machinery trade |
| CN112121452A (en) * | 2020-09-27 | 2020-12-25 | 江苏科技大学 | Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation |
| CN112274958A (en) * | 2020-09-28 | 2021-01-29 | 重庆前卫科技集团有限公司 | Ethylene glycol regeneration and recovery system and ethylene glycol recovery method in deep sea natural gas development process |
| CN213885035U (en) * | 2020-09-28 | 2021-08-06 | 重庆前卫科技集团有限公司 | Ethylene glycol regeneration and recovery system in deep sea natural gas development process |
Non-Patent Citations (2)
| Title |
|---|
| 三甘醇脱水技术在煤制天然气中影响因素的研究;仇登可;;辽宁化工(第09期);第1195页第2-7段 * |
| 番禺34-1气田乙二醇回收系统的设计改进;周生林;郭伟;宗俊斌;张海磊;刘红方;张强;郑天旭;;油气田地面工程(第06期);第34页第5段-第35页第12段 * |
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