CN112274958A - Ethylene glycol regeneration and recovery system and ethylene glycol recovery method in deep sea natural gas development process - Google Patents
Ethylene glycol regeneration and recovery system and ethylene glycol recovery method in deep sea natural gas development process Download PDFInfo
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- CN112274958A CN112274958A CN202011039637.3A CN202011039637A CN112274958A CN 112274958 A CN112274958 A CN 112274958A CN 202011039637 A CN202011039637 A CN 202011039637A CN 112274958 A CN112274958 A CN 112274958A
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 551
- 238000011069 regeneration method Methods 0.000 title claims abstract description 83
- 230000008929 regeneration Effects 0.000 title claims abstract description 82
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000003345 natural gas Substances 0.000 title claims abstract description 25
- 230000018109 developmental process Effects 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 58
- 150000003839 salts Chemical class 0.000 claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 17
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 17
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 12
- 230000018044 dehydration Effects 0.000 claims abstract description 11
- 238000010612 desalination reaction Methods 0.000 claims abstract description 11
- 239000011780 sodium chloride Substances 0.000 claims abstract description 10
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 9
- -1 salt ions Chemical class 0.000 claims abstract description 9
- 239000000243 solution Substances 0.000 claims description 131
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 63
- 238000001704 evaporation Methods 0.000 claims description 22
- 230000008020 evaporation Effects 0.000 claims description 22
- 239000000047 product Substances 0.000 claims description 20
- 238000010438 heat treatment Methods 0.000 claims description 16
- 239000007791 liquid phase Substances 0.000 claims description 14
- 239000012670 alkaline solution Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 10
- 239000002245 particle Substances 0.000 claims description 10
- 239000012071 phase Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 238000001556 precipitation Methods 0.000 claims description 6
- 238000005086 pumping Methods 0.000 claims description 6
- 238000011282 treatment Methods 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 238000011221 initial treatment Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000005191 phase separation Methods 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000003303 reheating Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 2
- 230000008719 thickening Effects 0.000 claims description 2
- 239000012535 impurity Substances 0.000 abstract description 4
- 239000003112 inhibitor Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000004677 hydrates Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D35/00—Filtering devices having features not specifically covered by groups B01D24/00 - B01D33/00, or for applications not specifically covered by groups B01D24/00 - B01D33/00; Auxiliary devices for filtration; Filter housing constructions
- B01D35/02—Filters adapted for location in special places, e.g. pipe-lines, pumps, stop-cocks
-
- 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
- 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
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- 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
- C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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Abstract
The invention discloses an ethylene glycol regeneration and recovery system in a deep sea natural gas development process, which comprises a pretreatment device responsible for removing light hydrocarbon and divalent salt ions in an ethylene glycol rich solution, a dehydration regeneration device responsible for removing water in the ethylene glycol rich solution and a desalination device responsible for removing monovalent salt in a saline ethylene glycol barren solution. The system realizes the separation of impurities such as light hydrocarbon, divalent salt ions, water, high-solubility salt and the like in the ethylene glycol rich liquid aiming at the ethylene glycol rich liquid obtained in the deep sea natural gas exploitation process, obtains the reusable ethylene glycol barren liquid, and saves the cost of deep sea natural gas exploitation. The invention also discloses an ethylene glycol recovery method of the ethylene glycol regeneration and recovery system in the deep sea natural gas development process.
Description
Technical Field
The invention relates to an ethylene glycol regeneration and recovery system and an ethylene glycol recovery method in a deep sea natural gas development process.
Background
In the process of developing a deep sea natural gas field, along with the increase of water depth, hydrates are easily formed in a submarine pipeline under the condition of high-pressure conveying, so that equipment such as a pipeline valve and the like are blocked, and the normal operation of production is influenced. Therefore, hydrate inhibitors, most commonly ethylene glycol, need to be added to prevent hydrate formation during natural gas development.
Ethylene glycol is used as an important organic chemical raw material, and due to economic considerations, the ethylene glycol rich solution used as an inhibitor generally needs to be regenerated and recycled to remove redundant moisture and impurities in the ethylene glycol rich solution so as to reduce the use cost. After part of produced liquid is absorbed when glycol for deep sea natural gas exploitation reflows from a pipeline, the glycol usually contains a certain amount of salts, and scaling and corrosion conditions are easy to occur in equipment, so that the whole process cannot work normally. However, the conventional ethylene glycol regeneration and recovery technology is lack of treatment for the above phenomena, so that an ethylene glycol recovery and regeneration system in deepwater oil and gas field development is in urgent need of development.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the system for regenerating and recovering the ethylene glycol rich solution specially used for the deep sea natural gas development is provided, so that various impurities in the ethylene glycol rich solution can be removed, and the ethylene glycol capable of being recycled can be obtained.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: the ethylene glycol regeneration and recovery system in the deep sea natural gas development process comprises a pretreatment device which is responsible for removing light hydrocarbon and divalent salt ions in ethylene glycol rich liquid, a dehydration regeneration device which is responsible for removing water in the ethylene glycol rich liquid and a desalination device which is responsible for removing monovalent salt in the saline ethylene glycol barren liquid,
the pretreatment device comprises an MEG tank for storing the ethylene glycol-rich solution from an upstream pipeline or facility, the MEG tank is connected with a flash tank preheater through a first delivery pump and a pipeline, the flash tank preheater is directly connected with the flash tank through a pipeline, and the flash tank is provided with an oil skimming tank connecting port positioned at the bottom of the tank and a pretreatment heater connecting port positioned at the lower part of the tank body; the pretreatment heater is respectively connected with the alkaline solution tank and the pretreatment tank through two pipelines, and the pretreatment tank is connected with the particle filter through a second delivery pump and a pipeline;
the outlet of the particle filter is directly communicated with an ethylene glycol rich liquid tank of the dehydration regeneration device through a pipeline, the ethylene glycol rich liquid tank is connected with a heat exchanger through a third transport pump and a pipeline, the heat exchanger is communicated with a regeneration tower through a pipeline, the bottom of the regeneration tower is directly connected with a vertical reboiler through a pipeline, and the outlet of the vertical reboiler is communicated with the middle part of the regeneration tower through a pipeline; the top of the regeneration tower is connected with a condenser through a pipeline, the bottom of the regeneration tower is communicated with a heat exchanger through a fifth transport pump and a pipeline, the condenser is connected with a separator through a pipeline, an outlet of the separator is communicated with a water tank through a pipeline, the top of the water tank is connected with a first vacuum pump through a pipeline, and the bottom of the water tank is connected with a fourth delivery pump;
a heat exchanger in the dehydration regeneration device is directly communicated with a salt-containing glycol barren solution tank in the desalination system through a pipeline, the salt-containing glycol barren solution tank is connected with a negative pressure flash tank through a sixth delivery pump and a pipeline, the top of the negative pressure flash tank is connected with a negative pressure condenser through a pipeline, the bottom of the negative pressure flash tank is respectively connected with a salt tank and a circulating heater through two pipelines, and an outlet of the circulating heater is communicated with the negative pressure flash tank through a pipeline; the outlet of the negative pressure condenser is connected with the ethylene glycol barren solution receiving tank through a pipeline, the top of the ethylene glycol barren solution receiving tank is connected with a second vacuum pump through a pipeline, and the bottom of the ethylene glycol barren solution receiving tank is connected with a qualified ethylene glycol barren solution storage tank through a seventh delivery pump and a pipeline.
As a preferable scheme, a torch connecting port positioned at the top of the flash tank is arranged on the flash tank, and the flash tank is connected with a torch through a pipeline.
Preferably, the separator is further provided with a pipeline communicated with the regeneration tower to convey the separated glycol solution into the regeneration tower.
The other technical problem to be solved by the invention is as follows: provides an ethylene glycol recovery method of the ethylene glycol rich solution regeneration and recovery system developed by the deep sea natural gas.
In order to solve the technical problems, the technical scheme adopted by the invention is as follows: the glycol recovery method of the glycol regeneration and recovery system in the deep sea natural gas development process comprises the following specific processes:
step 1: removing light hydrocarbon and divalent salt ions in ethylene glycol rich liquid
Step 1-1: collecting raw materials: when the sensor in the MEG tank measures that the liquid level of the ethylene glycol-rich solution in the tank reaches a specified height, the control system drives the first transportation pump to work;
step 1-2: preheating: preheating the ethylene glycol rich liquid by a flash tank preheater, and raising the temperature of the ethylene glycol rich liquid to 70-80 ℃ so as to meet the precondition of flash evaporation;
step 1-3: flash separation: the preheated ethylene glycol rich liquid enters a flash tank for flash evaporation to complete gas-liquid separation, and the separated hydrocarbon gas is transported to a torch through the top of the flash tank for combustion; residual non-condensable hydrocarbon substances are collected and recycled through an oil skimming tank at the bottom of the flash tank; discharging the ethylene glycol rich solution after hydrocarbon removal through a liquid phase outlet of the flash tank;
step 1-4: and (3) reheating: the temperature of the ethylene glycol rich liquid treated by the flash tank is reduced, and the ethylene glycol rich liquid is heated again through a liquid phase outlet of the flash tank by a pretreatment heater, so that the liquid temperature is increased to 70-80 ℃ again;
step 1-5: precipitation of low solubility salts: feeding the heated glycol rich solution into a pretreatment tank, and simultaneously adding an alkaline solution from an alkaline solution tank into the pretreatment tank to enable divalent salts in the glycol rich solution to react with the alkaline solution to form a precipitate;
step 1-6: solid-liquid separation: the second transportation pump operates, the solid-liquid mixture in the pretreatment tank is sent to a particle filter, and precipitated low-solubility salts are filtered to obtain a liquid-phase product after the glycol rich solution is subjected to primary treatment;
step 2: removing water in ethylene glycol rich liquid
Step 2-1: preheating: feeding the ethylene glycol rich solution obtained through the treatment in the steps 1-6 into a heat exchanger through a third transport pump for heating, so that the temperature of the ethylene glycol rich solution is raised to 80 +/-5 ℃;
step 2-2: and (3) cyclic heating: after entering a regeneration tower, the preheated glycol rich solution flows into a vertical reboiler from the bottom of the regeneration tower, the vertical reboiler externally heats the glycol rich solution to 139 +/-5 ℃ through a heat medium, and the heated glycol rich solution flows back into the regeneration tower again;
step 2-3: and (3) circulating rectification: after the ethylene glycol rich solution in the regeneration tower is heated to 139 +/-5 ℃, the light components in the ethylene glycol rich solution are separated from ethylene glycol gas-liquid, the ethylene glycol rich solution is continuously heated in a circulating way through a vertical reboiler, the light components in the ethylene glycol rich solution are continuously separated, the light components at the top of the regeneration tower are continuously concentrated, and the light components enter a condenser through a pipeline connected with the condenser at the top of the regeneration tower; thickening ethylene glycol at the tower bottom of the regeneration tower;
step 2-4: condensation and recovery: cooling a gas-phase product generated at the top of the regeneration tower to 30-40 ℃ through a condenser, refluxing about 3-6% of condensed water into the regeneration tower so as to be convenient for purifying ethylene glycol rich solution, and storing the rest condensed product into a water tank; then, pumping out a small amount of insoluble gas in the water tank through a first vacuum pump at the top of the water tank, and discharging the residual water in the water tank through a fourth transport pump;
step 2-5: cooling the saline glycol barren solution: the salt-containing glycol barren solution obtained through rectification in the step 2-3 is conveyed into a heat exchanger through a fifth conveying pump, and the salt-containing glycol barren solution with higher temperature is heated for preparing a glycol rich solution with lower temperature to be conveyed into a regeneration tower due to circulation heating, so that the temperature of the glycol rich solution is increased, and the energy required by heating in the step 2-2 is reduced;
and step 3: removing monovalent salt in lean solution of glycol containing salt
Step 3-1: flash evaporation: conveying the salt-containing glycol barren solution obtained in the step 2-5 into a negative pressure flash tank through a sixth conveying pump for flash evaporation, simultaneously heating the salt-containing glycol barren solution in the flash tank by a circulating heater, maintaining the temperature in the flash tank at 140 +/-5 ℃, and completing solid-gas-liquid three-phase separation of the salt-containing glycol barren solution in the negative pressure flash tank;
step 3-2: high solubility salt precipitation: the solubility of high-solubility monovalent salt in the liquid phase product after flash evaporation is reduced and is continuously separated out, and the high-solubility monovalent salt flows into a salt tank through a downcomer for storage, so that the ethylene glycol desalination process for exploiting deep sea natural gas is completed;
step 3-3: condensation: cooling the gas-phase product obtained by flash evaporation in the step 3-1 through a negative pressure condenser at the top of the flash evaporation tank, and then completely storing the gas-phase product into an ethylene glycol barren solution receiving tank;
step 3-4: separation: and pumping out a small amount of non-condensable gas by a second vacuum pump connected to the top of the ethylene glycol lean solution receiving tank, pumping out the ethylene glycol lean solution at the bottom of the ethylene glycol lean solution receiving tank from the bottom by a seventh transport pump, storing the ethylene glycol lean solution in a qualified ethylene glycol lean solution storage tank, and completing the regeneration and recovery of ethylene glycol.
The invention has the beneficial effects that:
the system aims at the ethylene glycol rich solution obtained by exploiting the deep sea natural gas, so that the separation of impurities such as light hydrocarbon, divalent salt ions, water, high-solubility salt and the like in the ethylene glycol rich solution is realized, the reusable ethylene glycol barren solution is obtained, and the cost of exploiting the deep sea natural gas is saved;
in the dehydration regeneration device, the salt-containing glycol barren solution with higher temperature is used for heating the low-temperature glycol rich solution through the heat exchanger, so that the cost for heating the glycol rich solution is saved, and the rectification efficiency of the glycol rich solution in the regeneration tower is improved;
because be equipped with the torch connector that is located tank deck portion on the flash tank, the flash tank is connected with the torch through the pipeline, can carry out combustion treatment with waste gas, avoids the polluted environment.
The storage tanks are arranged at the feeding sections of the three subsystems so as to prevent the change of the flow of the rich glycol solution inlet from influencing the driving of the system, thereby saving the running cost of the equipment.
Drawings
FIG. 1 is a system block diagram of the ethylene glycol regeneration and recovery of the present invention
In the figure: 1-pretreatment unit, 101-MEG tank, 102-first transfer pump, 103-flash tank and heater, 104-flash tank, 105-flare, 106-skimming tank, 107-pretreatment heater, 108-alkaline solution tank, 109-pretreatment tank, 110-second transfer pump, 111-particle filter;
2-dehydration regeneration device, 201-ethylene glycol rich liquor tank, 202-third transport pump, 203-heat exchanger, 204-regeneration tower, 205-vertical reboiler, 206-condenser, 207-separator, 208-water tank, 209-fourth transport pump, 210-first vacuum pump, 211-fifth transport pump;
3-desalination system, 301-saline ethylene glycol barren solution tank, 302-sixth delivery pump, 303-negative pressure flash tank, 304-circulating heater, 305-salt tank, 306-negative pressure condenser, 307-ethylene glycol barren solution receiving tank, 308-second vacuum pump, 309 seventh delivery pump, 310-qualified ethylene glycol barren solution storage tank.
Detailed Description
Specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
As shown in figure 1, the ethylene glycol regeneration and recovery system in the deep sea natural gas development process comprises a pretreatment device 1 which is responsible for removing light hydrocarbon and divalent salt ions in the ethylene glycol rich solution, a dehydration regeneration device 2 which is responsible for removing water in the ethylene glycol rich solution, and a desalination device 3 which is responsible for removing monovalent salt in the saline ethylene glycol barren solution,
the pretreatment device 1 comprises an MEG tank 101 for storing ethylene glycol-rich solution from an upstream pipeline or facility, the MEG tank 101 is connected with a flash tank preheater 103 through a first transfer pump 102 and a pipeline, the flash tank preheater 103 is directly connected with a flash tank 104 through a pipeline, and the flash tank 104 is provided with a flare 105 connecting port positioned at the top of the tank, a skimming tank connecting port positioned at the bottom of the tank and a pretreatment heater connecting port positioned at the lower part of the tank body; the pretreatment heater 107 is connected with the alkaline solution tank 108 and the pretreatment tank 109 through two pipelines respectively, and the pretreatment tank 109 is connected with the particle filter 111 through a second delivery pump 110 and a pipeline;
the outlet of the particle filter 111 is directly communicated with an ethylene glycol rich liquid tank 201 of the dehydration regeneration device 2 through a pipeline, the ethylene glycol rich liquid tank 201 is connected with a heat exchanger 203 through a third transportation pump 202 and a pipeline, the heat exchanger 203 is communicated with a regeneration tower 204 through a pipeline, the top of the regeneration tower 204 is connected with a condenser 206 through a pipeline, the bottom of the regeneration tower 204 is respectively communicated with the heat exchanger 203 through a fifth transportation pump 211 and a pipeline and is directly connected with a vertical reboiler 205 through a pipeline, and the outlet of the vertical reboiler 205 is communicated with the middle part of the regeneration tower 204 through a pipeline; the condenser 206 is connected with a separator 207 through a pipeline, an outlet of the separator 207 is respectively communicated with the regeneration tower 204 and a water tank 208 through two pipelines, the top of the water tank 208 is connected with a first vacuum pump 209 through a pipeline, and the bottom of the water tank 208 is connected with a fourth delivery pump 210;
the heat exchanger 202 in the dehydration regeneration device 2 is directly communicated with a salt-containing glycol barren solution tank in the desalination system 3 through a pipeline, the salt-containing glycol barren solution tank is connected with a negative pressure flash tank 303 through a sixth transfer pump and a pipeline, the top of the negative pressure flash tank 303 is connected with a negative pressure condenser 306 through a pipeline, the bottom of the negative pressure flash tank 303 is respectively connected with a salt tank 305 and a circulating heater 304 through two pipelines, and the outlet of the circulating heater 304 is communicated with the negative pressure flash tank 303 through a pipeline; an outlet of the negative pressure condenser 306 is connected with an ethylene glycol lean solution receiving tank 307 through a pipeline, the top of the ethylene glycol lean solution receiving tank 307 is connected with a second vacuum pump 308 through a pipeline, and the bottom of the ethylene glycol lean solution receiving tank 307 is connected with a qualified ethylene glycol lean solution storage tank through a seventh delivery pump 309 and a pipeline.
The glycol recovery method of the glycol regeneration and recovery system in the deep sea natural gas development process comprises the following specific processes:
step 1: removing light hydrocarbon and divalent salt ions in ethylene glycol rich liquid
Step 1-1: collecting raw materials: when a sensor in the MEG tank 101 measures that the liquid level of the ethylene glycol rich liquid stored in the tank reaches a specified height, the control system drives the first transportation pump 102 to work;
step 1-2: preheating: preheating the ethylene glycol rich liquid by a flash tank preheater 103, and raising the temperature of the ethylene glycol rich liquid to 70-80 ℃ so as to meet the precondition of flash evaporation;
step 1-3: flash separation: the preheated ethylene glycol rich liquid enters a flash tank 104 for flash evaporation to complete gas-liquid separation, and is transported to a torch 105 through the top of the flash tank 104 for combustion; the residual non-condensable hydrocarbon substances are collected, recycled and reused through an oil skimming groove 106 at the bottom of the flash tank 104; the ethylene glycol rich solution after hydrocarbon removal is discharged through a liquid phase outlet of the flash tank 104;
step 1-4: and (3) reheating: the temperature of the ethylene glycol rich liquid treated by the flash tank 104 is reduced, and the ethylene glycol rich liquid is heated again through a liquid phase outlet of the flash tank 104 by the pretreatment heater 107, so that the liquid temperature is increased to 70-80 ℃ again;
step 1-5: precipitation of low solubility salts: the heated liquid phase product after flash evaporation enters a pretreatment tank 109, and meanwhile, an alkaline solution is added into the pretreatment tank 109 from an alkaline solution tank 108, so that divalent salts in the ethylene glycol and the alkaline solution are subjected to chemical reaction to form a precipitate;
step 1-6: solid-liquid separation: the second transportation pump 110 is operated, the solid-liquid mixture in the pretreatment tank 109 is sent to the particle filter 111, and the precipitated low-solubility salts are filtered to obtain a liquid-phase product after the primary treatment of the glycol rich solution;
step 2: removing water in ethylene glycol rich liquid
Step 2-1: preheating: feeding the ethylene glycol rich solution obtained through the treatment in the steps 1-6 into a heat exchanger 203 through a third transport pump 202 for heating, so that the temperature of the ethylene glycol rich solution is increased to 80 ℃;
step 2-2: and (3) cyclic heating: after entering the regeneration tower 204, the preheated glycol rich solution flows into a vertical reboiler 205 from the bottom of the regeneration tower 204, the vertical reboiler 205 heats the glycol rich solution through hot steam outside until the temperature of the liquid in the regeneration tower 204 rises to 139 ℃, and the heated liquid flows back into the regeneration tower 204 again;
step 2-3: and (3) circulating rectification: after the temperature is reached, the liquid starts to be vaporized, water in the glycol rich solution enters a condenser 206 through the top of a regeneration tower 204, a heavier MEG solution at the bottom of the regeneration tower 204 is continuously heated circularly through a vertical reboiler 205 to concentrate the MEG solution, water in the MEG solution is removed, and glycol at the bottom of the regeneration tower is thickened;
step 2-4: condensation and recovery: the gas phase product generated by the regeneration tower 204 is cooled to 30-40 ℃ by a condenser 206, about 5% of condensed water flows back to the regeneration tower 204 for MEG solution purification, and the rest of condensed product is stored in a water tank 208; then, a small amount of insoluble gas in the water tank 208 is pumped out by the first vacuum pump 209 at the top of the water tank 208, and the remaining water in the water tank 208 is discharged by the fourth transport pump 210;
step 2-5: cooling the saline glycol barren solution: the salt-containing glycol barren solution obtained through rectification in the step 2-3 is conveyed into the heat exchanger 203 through the fifth transport pump 211, and the salt-containing glycol barren solution with higher temperature is heated for preparing the glycol rich solution with lower temperature conveyed into the regeneration tower 204 due to circulation heating, so that the temperature of the glycol rich solution is increased, and the energy required by heating in the step 2-2 is reduced;
and step 3: removing monovalent salt in lean solution of glycol containing salt
Step 3-1: flash evaporation: the saline ethylene glycol barren solution obtained in the step 2-5 is conveyed into a negative pressure flash tank 303 through a sixth conveying pump 302 for flash evaporation, meanwhile, a circulating heater 304 heats the ethylene glycol barren solution in the flash tank 303, the temperature in the flash tank is maintained at 140 +/-5 ℃, and the saline ethylene glycol barren solution completes solid-gas-liquid three-phase separation in the negative pressure flash tank 303;
step 3-2: high solubility salt precipitation: the high-solubility monovalent salt in the liquid phase product after flash evaporation is reduced in solubility and is continuously separated out, and the liquid phase product flows into the salt tank 305 through the downcomer for storage, so that the ethylene glycol desalination process for exploiting deep sea natural gas is completed;
step 3-3: condensation: cooling the gas-phase product obtained by the flash evaporation in the step 3-1 through a negative pressure condenser 306 at the top of the flash evaporation tank 303, and then completely storing the gas-phase product into an ethylene glycol barren solution receiving tank 307;
step 3-4: separation: a small amount of non-condensable gas is pumped out by a second vacuum pump 308 connected to the top of the ethylene glycol lean solution receiving tank 307, the ethylene glycol lean solution at the bottom in the ethylene glycol lean solution receiving tank 307 is pumped out from the bottom by a seventh transport pump 309, and the ethylene glycol lean solution is stored in a qualified ethylene glycol lean solution storage tank for storage, so that the regeneration and recovery of ethylene glycol are completed.
The above-mentioned embodiments are merely illustrative of the principles and effects of the present invention, and some embodiments may be used, not restrictive; it should be noted that, for those skilled in the art, various changes and modifications can be made without departing from the inventive concept of the present invention, and these changes and modifications belong to the protection scope of the present invention.
Claims (4)
1. A ethylene glycol regeneration and recovery system in the deep sea natural gas development process is characterized in that: comprises a pretreatment device which is responsible for removing light hydrocarbon and divalent salt ions in the glycol rich solution, a dehydration regeneration device which is responsible for removing water in the glycol rich solution and a desalination device which is responsible for removing monovalent salt in the saline glycol barren solution;
the pretreatment device comprises an MEG tank for storing the ethylene glycol-rich solution from an upstream pipeline or facility, the MEG tank is connected with a flash tank preheater through a first delivery pump and a pipeline, the flash tank preheater is directly connected with the flash tank through a pipeline, and the flash tank is provided with an oil skimming tank connecting port positioned at the bottom of the tank and a pretreatment heater connecting port positioned at the lower part of the tank body; the pretreatment heater is respectively connected with the alkaline solution tank and the pretreatment tank through two pipelines, and the pretreatment tank is connected with the particle filter through a second delivery pump and a pipeline;
the outlet of the particle filter is directly communicated with an ethylene glycol rich liquid tank of the dehydration regeneration device through a pipeline, the ethylene glycol rich liquid tank is connected with a heat exchanger through a third transport pump and a pipeline, the heat exchanger is communicated with a regeneration tower through a pipeline, the bottom of the regeneration tower is directly connected with a vertical reboiler through a pipeline, and the outlet of the vertical reboiler is communicated with the middle part of the regeneration tower through a pipeline; the top of the regeneration tower is connected with a condenser through a pipeline, the bottom of the regeneration tower is communicated with a heat exchanger through a fifth transport pump and a pipeline, the condenser is connected with a separator through a pipeline, an outlet of the separator is communicated with a water tank through a pipeline, the top of the water tank is connected with a first vacuum pump through a pipeline, and the bottom of the water tank is connected with a fourth delivery pump;
a heat exchanger in the dehydration regeneration device is directly communicated with a salt-containing glycol barren solution tank in the desalination system through a pipeline, the salt-containing glycol barren solution tank is connected with a negative pressure flash tank through a sixth delivery pump and a pipeline, the top of the negative pressure flash tank is connected with a negative pressure condenser through a pipeline, the bottom of the negative pressure flash tank is respectively connected with a salt tank and a circulating heater through two pipelines, and an outlet of the circulating heater is communicated with the negative pressure flash tank through a pipeline; the outlet of the negative pressure condenser is connected with the ethylene glycol barren solution receiving tank through a pipeline, the top of the ethylene glycol barren solution receiving tank is connected with a second vacuum pump through a pipeline, and the bottom of the ethylene glycol barren solution receiving tank is connected with a qualified ethylene glycol barren solution storage tank through a seventh delivery pump and a pipeline.
2. The system for ethylene glycol regeneration and recovery in the process of deep sea natural gas development as claimed in claim 1, wherein: the flash tank is provided with a torch connector positioned at the top of the tank, and the flash tank is connected with a torch through a pipeline.
3. The system for ethylene glycol regeneration and recovery in the process of deep sea natural gas development as claimed in claim 1, wherein: the separator is also provided with a pipeline which is communicated with the regeneration tower so as to input the separated glycol solution into the regeneration tower.
4. The ethylene glycol recovery method of the ethylene glycol regeneration and recovery system in the deep sea natural gas development process according to any one of claims 1 to 3, which comprises the following specific steps:
step 1: removing light hydrocarbon and divalent salt ions in ethylene glycol rich liquid
Step 1-1: collecting raw materials: when the sensor in the MEG tank measures that the liquid level of the ethylene glycol-rich solution in the tank reaches a specified height, the control system drives the first transportation pump to work;
step 1-2: preheating: preheating the ethylene glycol rich liquid by a flash tank preheater, and raising the temperature of the ethylene glycol rich liquid to 70-80 ℃ so as to meet the precondition of flash evaporation;
step 1-3: flash separation: the preheated ethylene glycol rich liquid enters a flash tank for flash evaporation to complete gas-liquid separation, and the separated hydrocarbon gas is transported to a torch through the top of the flash tank for combustion; residual non-condensable hydrocarbon substances are collected and recycled through an oil skimming tank at the bottom of the flash tank; discharging the ethylene glycol rich solution after hydrocarbon removal through a liquid phase outlet of the flash tank;
step 1-4: and (3) reheating: the temperature of the ethylene glycol rich liquid treated by the flash tank is reduced, and the ethylene glycol rich liquid is heated again through a liquid phase outlet of the flash tank by a pretreatment heater, so that the liquid temperature is increased to 70-80 ℃ again;
step 1-5: precipitation of low solubility salts: feeding the heated glycol rich solution into a pretreatment tank, and simultaneously adding an alkaline solution from an alkaline solution tank into the pretreatment tank to enable divalent salts in the glycol rich solution to react with the alkaline solution to form a precipitate;
step 1-6: solid-liquid separation: the second transportation pump operates, the solid-liquid mixture in the pretreatment tank is sent to a particle filter, and precipitated low-solubility salts are filtered to obtain a liquid-phase product after the glycol rich solution is subjected to primary treatment;
step 2: removing water in ethylene glycol rich liquid
Step 2-1: preheating: feeding the ethylene glycol rich solution obtained through the treatment in the steps 1-6 into a heat exchanger through a third transport pump for heating, so that the temperature of the ethylene glycol rich solution is raised to 80 +/-5 ℃;
step 2-2: and (3) cyclic heating: after entering a regeneration tower, the preheated glycol rich solution flows into a vertical reboiler from the bottom of the regeneration tower, the vertical reboiler externally heats the glycol rich solution to 139 +/-5 ℃ through a heat medium, and the heated glycol rich solution flows back into the regeneration tower again;
step 2-3: and (3) circulating rectification: after the ethylene glycol rich solution in the regeneration tower is heated to 139 +/-5 ℃, the light components in the ethylene glycol rich solution are separated from ethylene glycol gas-liquid, the ethylene glycol rich solution is continuously heated in a circulating way through a vertical reboiler, the light components in the ethylene glycol rich solution are continuously separated, the light components at the top of the regeneration tower are continuously concentrated, and the light components enter a condenser through a pipeline connected with the condenser at the top of the regeneration tower; thickening ethylene glycol at the tower bottom of the regeneration tower;
step 2-4: condensation and recovery: cooling a gas-phase product generated at the top of the regeneration tower to 30-40 ℃ through a condenser, refluxing about 3-6% of condensed water into the regeneration tower so as to be convenient for purifying ethylene glycol rich solution, and storing the rest condensed product into a water tank; then, pumping out a small amount of insoluble gas in the water tank through a first vacuum pump at the top of the water tank, and discharging the residual water in the water tank through a fourth transport pump;
step 2-5: cooling the saline glycol barren solution: the salt-containing glycol barren solution obtained through rectification in the step 2-3 is conveyed into a heat exchanger through a fifth conveying pump, and the salt-containing glycol barren solution with higher temperature is heated for preparing a glycol rich solution with lower temperature to be conveyed into a regeneration tower due to circulation heating, so that the temperature of the glycol rich solution is increased, and the energy required by heating in the step 2-2 is reduced;
and step 3: removing monovalent salt in lean solution of glycol containing salt
Step 3-1: flash evaporation: conveying the salt-containing glycol barren solution obtained in the step 2-5 into a negative pressure flash tank through a sixth conveying pump for flash evaporation, simultaneously heating the salt-containing glycol barren solution in the flash tank by a circulating heater, maintaining the temperature in the flash tank at 140 +/-5 ℃, and completing solid-gas-liquid three-phase separation of the salt-containing glycol barren solution in the negative pressure flash tank;
step 3-2: high solubility salt precipitation: the solubility of high-solubility monovalent salt in the liquid phase product after flash evaporation is reduced and is continuously separated out, and the high-solubility monovalent salt flows into a salt tank through a downcomer for storage, so that the ethylene glycol desalination process for exploiting deep sea natural gas is completed;
step 3-3: condensation: cooling the gas-phase product obtained by flash evaporation in the step 3-1 through a negative pressure condenser at the top of the flash evaporation tank, and then completely storing the gas-phase product into an ethylene glycol barren solution receiving tank;
step 3-4: separation: and pumping out a small amount of non-condensable gas by a second vacuum pump connected to the top of the ethylene glycol lean solution receiving tank, pumping out the ethylene glycol lean solution at the bottom of the ethylene glycol lean solution receiving tank from the bottom by a seventh transport pump, storing the ethylene glycol lean solution in a qualified ethylene glycol lean solution storage tank, and completing the regeneration and recovery of ethylene glycol.
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