WO2022062315A1 - 深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统及其脱盐方法 - Google Patents

深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统及其脱盐方法 Download PDF

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Publication number
WO2022062315A1
WO2022062315A1 PCT/CN2021/078290 CN2021078290W WO2022062315A1 WO 2022062315 A1 WO2022062315 A1 WO 2022062315A1 CN 2021078290 W CN2021078290 W CN 2021078290W WO 2022062315 A1 WO2022062315 A1 WO 2022062315A1
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tank
negative pressure
salt
valve
temperature
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PCT/CN2021/078290
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English (en)
French (fr)
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唐文献
何佳伟
齐继阳
薛少锋
刘波
王�锋
肖尊坤
李华
张建
陈晨
王文涛
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江苏科技大学
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Publication of WO2022062315A1 publication Critical patent/WO2022062315A1/zh

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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
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • 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
    • 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

Definitions

  • the invention relates to a desalination system and a desalination method for ethylene glycol lean liquid containing high-solubility salt in deep-sea natural gas exploitation.
  • Ethylene glycol is often used as a hydrate inhibitor due to its low volatility and easy separation from water.
  • MRU ethylene glycol regeneration and recovery system
  • the glycol solution returning from the pipeline usually contains a certain amount of salts after absorbing part of the produced fluid.
  • the traditional ethylene glycol recovery technology is difficult to remove salts in ethylene glycol.
  • the salt is easily deposited on the inner surface of the container in the regeneration process during the regeneration and recovery of ethylene glycol, causing scaling and clogging of the pipeline. Causes the whole process to not work properly.
  • the produced fluid has high salt content, and the existing methods are not enough to remove the salt content; the same problem also exists in the development of onshore gas fields.
  • the regeneration system was not desalinated, resulting in fouling and clogging in the reboiler.
  • the technical problem to be solved by the present invention is to provide a desalination system capable of efficiently removing high-solubility salt ions in the lean ethylene glycol solution.
  • the technical scheme adopted in the present invention is: a desalination system containing high-solubility salt ethylene glycol lean liquid in deep-sea natural gas exploitation, including MEG lean liquid recovery device, salt-containing glycol lean liquid flash evaporation device and a first-order salt recovery device;
  • the salt-containing ethylene glycol lean liquid flashing device comprises a salt-containing ethylene glycol lean liquid tank, which is connected with the first transport pump through a pipeline, and the pipeline between the salt-containing ethylene glycol lean liquid tank and the first transport pump A first shut-off valve is installed on it, the first transport pump is connected to the negative pressure flash tank through a pipeline, and a first check valve, a first one-way valve, a second one-way valve are installed on the pipeline between the first transport pump and the negative pressure flash tank.
  • An electric valve and a first flow control valve a first temperature transmitter is installed on the pipeline between the first transport pump and the one-way valve, and a first temperature transmitter is installed on the pipeline between the electric valve and the flow control valve
  • a flow transmitter and a first flow controller the negative pressure flash tank is provided with two liquid phase outlets and one gas phase outlet located at the top of the tank, the gas phase outlet is connected to the negative pressure condenser through a pipeline, and one liquid phase outlet is The liquid pipe is connected to the salt liquid tank, the other liquid phase outlet is connected to the circulation heater through the second transport pump, and the outlet of the circulation heater is connected to the negative pressure flash tank to form a closed loop;
  • a first pressure controller, a second pressure transmitter and a first pressure gauge are installed on the negative pressure flash tank for real-time monitoring and control of the pressure in the negative pressure flash tank, and the negative pressure flash tank is also installed
  • There is a thermometer and a temperature calibrator, a fourth pressure transmitter and a fifth one-way valve are installed on the pipeline between the negative pressure flash tank and the second transport pump, and the second transport pump and the circulation heater are installed
  • the sixth one-way valve and the seventh one-way valve are arranged on the pipeline between the sixth one-way valve and the seventh one-way valve
  • the fifth pressure transmitter and the third temperature gauge are arranged on the pipeline between the sixth one-way valve and the seventh one-way valve.
  • the outlet of the circulating heater is connected to the negative pressure flash tank through the pipeline with the eighth one-way valve, and the pipeline between the eighth one-way valve and the negative pressure flash tank is installed to ensure the heated MEG Lean liquid temperature and the second pressure controller, the fourth temperature meter, the fourth temperature transmitter and the fifth temperature meter that reach the specified value;
  • the salt-containing ethylene glycol lean liquid flashing device includes a negative pressure condenser communicated with the negative pressure flash tank through the pipeline provided with the second one-way valve, and the pipeline between the negative pressure flash tank and the negative pressure condenser is on the pipeline.
  • a first differential pressure transmitter, a second pressure gauge and a second temperature transmitter are installed; the negative pressure condenser is connected to the MEG lean liquid receiving tank through the pipeline provided with the third one-way valve and the second electric valve, and the pipeline
  • a third pressure gauge is installed between the negative pressure condenser and the third one-way valve, and the pipeline between the second electric valve and the MEG lean liquid receiving tank is arranged to confirm the MEG lean liquid obtained after flashing.
  • the MEG lean liquid receiving tank is provided with a third pressure transmitter, a second temperature gauge and Liquid level meter;
  • the top of the MEG lean liquid receiving tank is provided with a gas phase outlet, which is connected to the vacuum pump through a pipeline with a vacuum valve, and the liquid phase outlet at the bottom of the MEG lean liquid receiving tank is connected to the third transport pump through the third stop valve.
  • a second bypass valve is connected between the inlet of the third transport pump and the outlet of the third transport pump, and the third transport pump is communicated with the qualified MEG lean liquid storage tank through the fourth one-way valve;
  • the monovalent salt recovery system includes a water tank.
  • the water tank is communicated with the salt solution tank through a pipeline provided with a fourth transport pump, and a tenth one-way is sequentially installed on the pipeline between the outlet of the fourth transport pump and the salt solution tank.
  • valve, the fourth electric valve and the second flow control valve ;
  • a fourth pressure gauge is installed on the pipeline between the fourth transport pump and the one-way valve, and
  • a pressure gauge is installed on the pipeline between the electric valve and the flow control valve
  • the second flow transmitter and the second flow controller are used to control the concentration of the salt solution in the salt solution tank to control the amount of water inflow; between the negative pressure flash tank and the salt solution tank, a ninth one-way valve and a third electric valve are arranged in turn.
  • the pipes are connected to each other, and the salt solution tank is equipped with a seventh temperature gauge, a second liquid level transmitter, and a second liquid level control device to monitor the concentration of the salt solution in the salt solution tank in real time and maintain the stability of the liquid level in the salt solution tank.
  • a seventh temperature gauge to monitor the concentration of the salt solution in the salt solution tank in real time and maintain the stability of the liquid level in the salt solution tank.
  • device a fifth pressure gauge and a second conductivity meter;
  • the salt solution tank is connected to the fifth transport pump through two parallelly arranged pipelines with the fifth shut-off valve and the fifth bypass valve, and an eleventh unit is connected to the pipeline between the fifth transport pump and the centrifuge.
  • the centrifuge is provided with a gas-phase outlet at the top and a solid-phase outlet at the bottom, wherein the gas-phase outlet at the top communicates with the outside through a pipeline with a thirteenth one-way valve, and the solid-phase outlet at the bottom
  • the pipeline of the fourteenth one-way valve communicates with the salt tank.
  • the output port of the first transport pump is also connected to the pipeline between the salt-containing glycol lean liquid tank and the first shut-off valve through the pipeline provided with the first bypass valve to form a first bypass.
  • a first pressure transmitter is installed on the pipeline between the loop connection port of the first bypass loop and the first shut-off valve.
  • the negative pressure flash tank is provided with a first liquid level transmitter and a first liquid level transmitter for controlling the lowest liquid level to ensure a stable amount of MEG lean liquid flashed in the tank. Bit controller.
  • a second differential pressure transmitter is connected between the pipeline at the outlet end of the sixth one-way valve and the pipeline at the outlet end of the seventh one-way valve.
  • the fourth transport pump constitutes a bypass circuit through a pipeline provided with a fourth stop valve and a fourth bypass valve.
  • the centrifuge is provided with a circulation loop outlet at the bottom, and the circulation loop outlet is connected to the salt solution tank through a pipeline provided with a twelfth one-way valve and a sixth electric valve.
  • the system efficiently realizes the desalination recovery and reuse of the salt-containing ethylene glycol lean liquid used for deep-sea natural gas exploitation, and greatly reduces the loss of ethylene glycol to reduce the cost of use;
  • the monovalent salt NACL crystals in the lean liquid are extracted, which can be used for subsequent deep processing, which improves the economic benefit.
  • the first flow transmitter and the first flow controller are installed on the pipeline between the electric valve and the flow control valve, it can be adjusted according to the pressure, liquid level, temperature and other information in the negative pressure flash tank.
  • the second pressure controller, the fourth temperature gauge, the fourth temperature transmitter and the fifth temperature gauge are installed on the pipeline between the eighth one-way valve and the negative pressure flash tank, it can ensure that the heating After the MEG lean liquid temperature reaches the specified value.
  • the MEG lean liquid receiving tank is provided with a third pressure transmitter, a second temperature gauge and a liquid level meter, the pressure, temperature and liquid level in the tank can be monitored. Since the seventh temperature gauge, the second liquid level transmitter, the second liquid level controller, the fifth pressure gauge and the second conductivity meter are arranged on the salt solution tank, the concentration of the salt solution in the salt solution tank can be monitored in real time. And keep the liquid level in the salt solution tank stable.
  • the material and liquid transportation in this system adopts the method of bypass loop, which can ensure the stability of the pipeline in the process of transporting the solution and improve the safety of the whole system.
  • Another technical problem to be solved by the present invention is to provide a desalination method for the desalination system of the ethylene glycol lean liquid containing high solubility salt in the above-mentioned deep-sea natural gas exploitation.
  • the technical scheme adopted in the present invention is: a desalination method of a desalination system containing a high-solubility salt ethylene glycol lean liquid for deep-sea natural gas exploitation, and the specific process is as follows:
  • Step 1 flash evaporation of salty glycol lean liquid:
  • Step 1-1 raw material transportation: in the initial state, the valves in each system are closed; first open the first stop valve and the first bypass valve, start the first transportation pump, when the salt-containing ethylene glycol lean liquid tank After the bypass circuit between it and the first transport pump is filled with MEG lean liquid, the first pressure transmitter detects that the pressure in the pipe is stable, then opens the electric valve through remote control, opens the first flow control valve, and closes the first bypass. Through the valve, the raw material of the salt-containing ethylene glycol lean liquid is transported to the negative pressure flash tank;
  • Step 1-2 flow control: when the first liquid level transmitter on the negative pressure flash tank detects that the solution in the tank reaches the specified liquid level, the first flow control valve on the feed pipe is controlled by the control system to adjust The flow rate in the tank is large, and the liquid level of the negative pressure flash tank is kept stable; if there is an emergency situation, the first electric valve will be directly closed remotely to prevent the inflow of raw materials;
  • Step 1-3 circulating heating: the salt-containing ethylene glycol lean liquid flowing into the negative pressure flash tank is transferred to the circulating heater for heating through the second transport pump and then flows back to the negative pressure flash tank, which is located in the negative pressure flash tank.
  • the temperature calibrator on the pressure flash tank and the fourth temperature transmitter monitor the temperature in the tank in real time to ensure that the temperature in the tank is stable at 140 ⁇ 5°C;
  • Steps 1-4 flash: the first pressure controller and the second pressure transmitter on the negative pressure flash tank ensure that the operating pressure of the negative pressure flash tank is maintained at 15 ⁇ 5KPa; due to the drop in pressure, the negative pressure flash The ethylene glycol in the evaporation tank starts to be flashed and separated, and the temperature is supplemented by the circulating heating circuit to maintain the temperature required in the flash evaporation process.
  • the MEG lean liquid is distilled out and accumulated in the gas phase in the negative pressure flash tank. top;
  • Step 2-1 MEG lean liquid condensation:
  • the MEG lean liquid gas generated by flashing enters the negative pressure condenser through the second one-way valve, and the hot steam is rapidly cooled to 40 ⁇ 3°C to reliquefy the MEG lean liquid gas. Then open the second electric valve to condense the condensate into the MEG lean liquid receiving tank;
  • Step 2-2 purification: open the vacuum valve and pneumatic vacuum pump, discharge a small amount of gas in the MEG lean liquid receiving tank, and store the remaining MEG lean liquid in the qualified MEG lean liquid storage tank through the third transport pump;
  • Step 3-1 salt solution storage: the salt solution at the bottom of the negative pressure flash tank obtained in step 1-4 is transported to the salt solution tank through the downcomer, and the monovalent salt in the salt solution tank has reached saturation. After the salt concentration in the salt solution tank reaches the set value measured by the second conductivity measuring instrument, it is transported to the centrifuge by the fifth transport pump for centrifugation;
  • Step 3-2 centrifugal separation: some insoluble gas mixed in the salt solution sent to the centrifuge is discharged through the thirteenth one-way valve above the centrifuge. After the remaining solid-liquid mixture is centrifuged, the solid salt block is stored in the salt tank It is stored in the medium and used as the raw material for subsequent deep processing, and the remaining incompletely centrifuged solution flows back into the salt solution tank through the liquid phase outlet of the centrifuge;
  • Step 3-3 water injection: when the second liquid level transmitter detects that the liquid level in the salt liquid tank drops to the lower limit, the second liquid level controller sends a signal to control the system to open the fourth electric valve Pump water from the tank and inject it into the salt solution tank to ensure the stability of the liquid level in the salt solution tank; when the second conductivity meter measures the salt concentration in the salt solution tank to be lower than the set value, stop the centrifuge and close it.
  • the liquid level in the negative pressure flash tank is set with high liquid level limit alarm, high liquid level alarm, low liquid level alarm and low liquid level limit through the liquid level transmitter.
  • Alarm when the liquid level is not within the normal range, causing the above alarms to be triggered, deal with the following methods:
  • the high liquid level limit alarm is triggered, and the first electric valve in the feeding circuit is cut off to prevent the salt-containing glycol lean liquid from immersing and defogging. After that, with the continuation of the distillation process, the liquid level in the negative pressure flash tank drops to the point where the low liquid level alarm is triggered, and then the feed circuit is reopened;
  • the circulating heater When the liquid level in the negative pressure flash tank is too low and the liquid level limit is too low alarm, the circulating heater will be turned off urgently to control the temperature of the salt-containing ethylene glycol lean liquid in the negative pressure flash tank below 170°C; After that, the salt-containing ethylene glycol lean liquid newly injected into the negative pressure flash tank will have a slow distillation process due to insufficient heating, and the liquid level in the negative pressure flash tank will gradually increase. When the alarm is too high, restart the circulating heater;
  • the high liquid level alarm is triggered.
  • the low liquid level in the flash tank under negative pressure triggers the low liquid level alarm, adjust the opening of the first flow control valve in the feed circuit to the maximum; if the feed flow has reached the maximum, reduce the work of the circulating heater temperature to the set operating temperature value, thereby reducing the distillation rate.
  • the pressure transmitter on the upper part of the negative pressure flash tank is provided with an alarm for too high pressure, an alarm for too low pressure and an alarm for too high pressure limit.
  • the pressure in the negative pressure flash tank is not within the normal range , when the corresponding alarm is triggered, it is handled as follows:
  • the temperature transmitter in the negative pressure flash tank is set with a low temperature alarm, an excessive temperature alarm, and an excessive temperature limit alarm.
  • the temperature in the negative pressure flash tank is not in the normal range
  • the corresponding alarm is triggered, it is handled as follows:
  • the circulating heater is adjusted to work under the condition that the heating value is the upper limit of the set working temperature, so that the negative pressure flash tank will work.
  • the solution in the system is heated up to the set normal range as soon as possible; if the circulating heater has been working under the condition that the heating value is the upper limit of the set working temperature, reduce the opening of the first flow control valve on the feeding circuit to make the feeding reduced flow;
  • the circulating heater is turned off immediately and waits for the operator to intervene.
  • the circulating heater when the density of the MEG lean liquid measured in real time by the density indicator in the MEG lean liquid receiving tank is less than the set lower limit value, check whether the circulating heater is activated and its heating value is the set working temperature The upper limit value, if it is not started or the heating value does not reach the upper limit value of the set working temperature, the circulating heater will be heated up to the upper limit value of the set working temperature, so as to speed up the salt-containing ethylene glycol in the negative pressure flash tank. The distillation speed of the alcohol-depleted liquid; if the circulating heater has been started at this time, and the heating capacity of the circulating heater reaches the upper limit of the set working temperature, then reduce the opening of the first flow control valve in the feeding loop.
  • the circulating heater When the density of the MEG lean liquid in the MEG lean liquid receiving tank measured in real time is less than the qualified value, check whether the circulating heater is activated and its heating value is the upper limit of the set working temperature. If it is not activated or the heating value If the upper limit of the set working temperature is not reached, make the circulating heater work according to the heating value of the upper limit of the set working temperature, so as to speed up the distillation speed of the salt-containing ethylene glycol lean liquid in the negative pressure flash tank; At this time, the circulating heater has been started, and the heating capacity of the circulating heater reaches the upper limit of the set working temperature, then reduce the opening of the first flow control valve in the feeding loop to reduce the drop of the feeding speed and increase the negative pressure. Separation efficiency of flash tank.
  • the method enables the desalination system to complete the desalination operation of the ethylene glycol lean liquid containing high-solubility salts in deep-sea natural gas exploitation, and the ethylene glycol recovery rate is high, and the operation is safe and reliable.
  • step 1-1 raw material transportation, open the first flow control valve and close the first bypass valve at the same time, so as to transport the raw material of about 95°C salt-containing ethylene glycol lean liquid into the negative pressure flash tank, which can prevent direct opening
  • the valve transportation has an impact on the mechanism
  • step 2-2 since the MEG lean liquid gas will inevitably be mixed with a small amount of non-condensable gas during the condensation process, it will be merged into the MEG lean liquid receiving tank together with the condensed liquid, so open the vacuum valve and pneumatic vacuum pump to reduce the MEG lean liquid. A small amount of gas in the liquid receiving tank is discharged;
  • step 3-2 centrifugal separation, some insoluble gas mixed in the salt solution sent to the centrifuge is discharged through the thirteenth one-way valve above the centrifuge. After the remaining solid-liquid mixture is centrifuged, the solid salt block is stored in the salt It is stored in the tank as raw material for subsequent deep processing, and the remaining incompletely centrifuged solution is returned to the salt solution tank through the liquid phase outlet of the centrifuge, which not only replenishes the liquid level of the salt solution tank, but also participates in centrifugation again to reduce the loss of ethylene glycol. ;
  • step 3-3 once the salt solution in the salt solution tank meets the centrifugation requirements, the continuous centrifugation will lead to the continuous drop of the liquid level in the tank, which may endanger the stability of the entire system, so when the second liquid level transmitter When it is detected that the liquid level in the salt liquid tank drops to the lower limit, the second liquid level controller sends a signal to control the system to open the fourth electric valve, and pump water from the water tank into the salt liquid tank to ensure that the salt liquid tank is in the The liquid level is stable; at the same time, water injection will also reduce the salt concentration of the solution in the salt liquid tank.
  • the first pressure controller and the second pressure transmitter on the negative pressure flash tank ensure that the operating pressure of the negative pressure flash tank is maintained at 15 ⁇ 5KPa; when the pressure in the negative pressure flash tank is maintained After the temperature reaches the set value, the monovalent salt is saturated in the ethylene glycol liquid, and the salt-containing ethylene glycol lean liquid starts to be flashed and separated, and the temperature is supplemented through the circulating heating circuit to maintain the temperature in the flash evaporation process. At the required temperature, the MEG lean liquid is distilled out and stacked on the top of the negative pressure flash tank in the form of gas phase, which improves the efficiency of flash desalination.
  • the solution may submerge the mist eliminator installed on the top of the negative pressure flash tank, corrode it and cause it to fail to work normally; if the liquid level is too low, it means that the negative pressure flash evaporation
  • the lack of salt-containing ethylene glycol lean liquid in the tank will affect the normal operation of other equipment in the experimental device, resulting in low overall operation efficiency of the experimental system and affecting the experimental results.
  • the method effectively realizes the liquid level control in the negative pressure flash tank.
  • Fig. 1 is the layout diagram of the desalination system of the present invention.
  • FIG. 1 1-Salt glycol lean liquid tank, 2-First transport pump, 3-Negative pressure flash tank, 4-Second transport pump, 5-Circulation heater, 6-Negative pressure condenser, 7-MEG lean liquid receiving tank, 8-vacuum pump, 9-third transport pump, 10-qualified MEG lean liquid storage tank, 11-water tank, 12-fourth transport pump, 13-salt liquid tank, 14-fifth Transport pump, 15-centrifuge, 16-salt tank;
  • S1-first pressure transmitter S2-first temperature transmitter, S3-first flow transmitter, S4-first flow controller, S5-first pressure controller, S6-second pressure transmitter device, S7-first pressure gauge, S8-first liquid level transmitter, S9-first liquid level controller, S10-first temperature gauge, S11-temperature calibrator, S12-first differential pressure transmitter device, S13-second temperature transmitter, S14-second pressure gauge, S15-third pressure gauge, S16-first conductivity meter, S17-third temperature transmitter, S18-temperature controller, S19 - 3rd pressure transmitter, S20 - 2nd temperature gauge, S21 - level gauge, S22 - 4th pressure transmitter, S23 - 5th pressure transmitter, S24 - 3rd temperature gauge, S25 - 2nd Differential pressure transmitter, S26-second pressure controller, S27-fourth temperature gauge, S28-fourth temperature transmitter, S29-fifth temperature gauge, S30-sixth temperature gauge, S31-fourth pressure gauge , S32- second flow transmitter
  • a desalination system for ethylene glycol lean liquid containing high-solubility salts in deep-sea natural gas exploitation includes a MEG lean liquid recovery device, a salt-containing ethylene glycol lean liquid flash evaporation device, and a first-order salt recovery device;
  • the salt-containing ethylene glycol lean liquid flash evaporation device comprises a salt-containing glycol lean liquid tank 1, which is connected to the first transport pump 2 through a pipeline, and the salt-containing glycol lean liquid tank 1 and the first transport pump 2
  • a first shut-off valve V1 is installed on the pipeline between them, and a three-way valve is connected to the output port of the first transport pump 2.
  • One of the three-way valves is connected to the salt-containing ethylene glycol through the pipeline with the first bypass valve V2.
  • a first bypass loop is formed on the pipeline between the lean liquid tank and the first cut-off valve V1, and a first pressure transmitter is installed on the pipeline between the loop connection port of the first bypass loop and the first cut-off valve V1 S1;
  • the first transport pump 2 is connected to the negative pressure flash tank 3 through a pipeline, and the pipeline between the first transport pump 2 and the negative pressure flash tank 3 is sequentially installed with a first check valve V3, a first one-way valve
  • the electric valve V4 and the first flow control valve V5 a first temperature transmitter S2 is installed on the pipeline between the first transport pump 2 and the one-way valve V3, and the first temperature transmitter S2 is installed between the electric valve V4 and the flow control valve V5.
  • a first flow transmitter S3 and a first flow controller S4 are installed on the pipeline, which can adjust the flow rate in the transport pipe according to the pressure, liquid level, temperature and other information in the negative pressure negative pressure flash tank 3;
  • the flash tank is provided with two liquid-phase outlets and a gas-phase outlet located at the top of the tank, the gas-phase outlet is connected to the negative pressure condenser 6 through a pipeline, one of the liquid-phase outlets is connected to the salt liquid tank 13 through a downcomer, and the other liquid-phase outlet is
  • the second transport pump 4 is connected to the circulating heater 5 and the outlet of the circulating heater 5 is connected to the negative pressure flash tank 3 to form a closed loop;
  • a first pressure controller S5, a second pressure transmitter S6 and a first pressure gauge S7 are installed on the negative pressure flash tank 3 to monitor and control the pressure in the negative pressure flash tank 3 in real time.
  • the tank 3 is also provided with a temperature gauge S10 and a temperature calibrator S11, and the lower part of the inner side of the tank body of the negative pressure flash tank 3 is provided with a first level that controls the minimum liquid level to ensure the stability of the amount of MEG lean liquid flashed in the tank.
  • a fifth pressure transmitter S23 and a third temperature gauge S24 are arranged on the pipeline of the boiler; the outlet of the circulating heater 5 is connected to the negative pressure flash tank 3 through the pipeline provided with the eighth one-way valve V16, and the sixth one-way valve V14
  • a second differential pressure transmitter S25 is connected between the pipeline at the outlet end and the pipeline at the outlet end of the seventh one-way valve V15, and a second differential pressure transmitter S25 is installed on the pipeline between the eighth one-way valve V16 and the negative pressure flash tank 3 to ensure that the The heated MEG lean liquid temperature and the second pressure controller
  • the MEG recovery system includes a negative pressure condenser 6 that communicates with the negative pressure flash tank 3 through the pipeline provided with the second check valve V6, and the pipeline between the negative pressure flash tank 3 and the negative pressure condenser 6 is installed There are the first differential pressure transmitter S12, the second pressure gauge S14 and the second temperature transmitter S13; the negative pressure condenser 6 is connected to the MEG lean liquid through the pipeline provided with the third one-way valve V7 and the second electric valve V8 In the receiving tank 7, a third pressure gauge S15 is installed between the negative pressure condenser 6 and the third one-way valve V7 on the pipeline, and it is useful to arrange the pipeline between the second electric valve V8 and the MEG lean liquid receiving tank 7 In order to confirm the first conductivity measuring instrument S16, the third temperature transmitter S17 and the temperature controller S18 of the high solubility monovalent salt ion content in the MEG lean liquid obtained after flashing; on the MEG lean liquid receiving tank 7 A third pressure transmitter S19, a second temperature gauge S20 and
  • the monovalent salt recovery system includes a water tank 11, and the water tank 11 communicates with the salt solution tank 13 through a pipeline provided with a fourth transport pump 12, and the fourth transport pump 12 is provided with a fourth shut-off valve V19 and a fourth bypass valve V20.
  • the pipeline constitutes a bypass circuit; a tenth one-way valve V21, a fourth electric valve V22 and a second flow control valve V23 are sequentially installed on the pipeline between the outlet of the fourth transport pump 12 and the salt solution tank 13;
  • a fourth pressure gauge S31 is installed on the pipeline between the four transport pumps 12 and the one-way valve V21, and the pipeline between the electric valve V22 and the flow control valve V23 is installed to control the flow rate according to the concentration of the salt solution in the salt solution tank 13.
  • the salt solution tank 13 is arranged with a seventh thermometer S34, a second liquid level transmitter S35, a second liquid level transmitter S35 for monitoring the concentration of the salt solution in the salt solution tank 13 in real time and maintaining a stable liquid level in the salt solution tank 13 Bit controller S36, fifth pressure gauge S37 and second conductivity measuring instrument S38;
  • the tank 13 is connected to the fifth transport pump 14 through two parallelly arranged pipelines with the fifth shut-off valve V24 and the fifth bypass valve V25, and the pipeline between the fifth transport pump 14 and the centrifuge 15 is connected with a second pump.
  • the eleventh one-way valve V26 and the fifth electric valve V27, the sixth pressure transmitter S39 is provided on the pipeline between the transport pump 14 and the one-way valve V26, and the pipeline between the fifth electric valve V27 and the centrifuge 15 is provided
  • a third flow transmitter S40 and a third flow controller S41 are provided; the centrifuge 15 is provided with a gas-phase outlet at the top, a solid-phase outlet at the bottom and a circulation loop outlet, wherein the gas-phase outlet at the top is provided with a tenth
  • the pipeline of the three-way valve V30 is communicated with the outside world, the solid phase outlet at the bottom is connected to the salt tank 16 through the pipeline provided with the fourteenth one-way valve V31, and the outlet of the circulation loop is set through the t
  • the desalination method of the desalination system of the ethylene glycol lean liquid containing high solubility salt in deep sea natural gas exploitation is as follows:
  • Step 1 flash evaporation of salty glycol lean liquid:
  • Step 1-1 raw material transportation: in the initial state, the valves in each system are closed; first open the first stop valve V1 and the first bypass valve V2, start the first transportation pump 2, when the salt-containing ethylene glycol
  • the first pressure transmitter S1 detects that the pressure in the pipe is stable, and then opens the electric valve V4 through remote control, and opens the first flow control valve V5, close the first bypass valve V2 at the same time, and transport the raw material of the salt-containing ethylene glycol lean liquid at about 95°C to the negative pressure flash tank 3, which can prevent the impact on the mechanism caused by directly opening the valve for transportation;
  • Step 1-2 flow control: when the first liquid level transmitter S8 on the negative pressure flash tank 3 detects that the solution in the tank reaches the specified liquid level, the first flow control valve on the feeding pipe is controlled by the control system V5, adjust the flow rate in the tank to keep the liquid level of the negative pressure flash tank 3 stable; if there is an emergency situation, the first electric valve V4 will be directly and remotely closed to prevent the inflow of raw materials;
  • Steps 1-3 circulating heating: the 95°C salt-depleted ethylene glycol feed liquid cannot meet the requirements of flash evaporation in the negative pressure flash tank, so it needs to be heated.
  • the salt-containing ethylene glycol lean liquid flowing into the negative pressure flash tank 3 is transferred to the circulating heater 5 for heating by the second transport pump 4 and flows back into the negative pressure flash tank 3 again, which is located in the negative pressure flash tank.
  • the temperature calibrator S11 on the 3 and the fourth temperature transmitter S28 monitor the temperature in the tank in real time to ensure that the temperature in the tank is stable at 140 ⁇ 5°C;
  • Steps 1-4 flashing not only requires the temperature to reach a certain value, but also has requirements for the pressure.
  • the first pressure controller S5 and the second pressure transmitter S6 on the negative pressure flash tank ensure that the negative pressure flash tank The operating pressure is maintained at 15 ⁇ 5KPa; when the pressure and temperature in the negative pressure flash tank reach the set value, the monovalent salt NaCl reaches a saturated state in the ethylene glycol solution, and the salty ethylene glycol lean solution begins to flash Evaporation, through continuous circulating heating, the MEG lean liquid is distilled out and stacked on the top of the negative pressure flash tank 3 in the form of a gas phase, and more than 90% of the solution at the bottom of the remaining negative pressure flash tank 3 is a monovalent salt solution;
  • Step 2-1 MEG lean liquid condensation:
  • the MEG lean liquid gas generated by flashing enters the negative pressure condenser through the second check valve V6, and the hot steam is rapidly cooled to 40 ⁇ 3°C so that the MEG lean liquid gas is reliquefied , and then open the second electric valve V8, and the condensate is fed into the MEG lean liquid receiving tank 7;
  • Step 2-2 purification: Since the MEG lean liquid gas will inevitably be mixed with a small amount of non-condensable gas during the condensation process, it will be merged into the MEG lean liquid receiving tank together with the condensed liquid, so open the vacuum valve V9 and the pneumatic vacuum pump 9. A small amount of gas in the lean liquid receiving tank is discharged, and the remaining MEG lean liquid is stored in the qualified MEG lean liquid storage tank 10 through the third transport pump 9, and is used again as an inhibitor used in the marine natural development process;
  • Step 3-1 salt solution storage: the salt solution at the bottom of the negative pressure flash tank 3 obtained in step 1-4 is transported to the salt solution tank 13 through the downcomer, and the monovalent salt in the salt solution tank 13 If NaCl etc. have reached the saturated state, crystallization begins, and after the second conductivity measuring instrument S38 measures that the salt concentration in the salt solution tank 13 reaches the set value, it is transported to the centrifuge 15 by the fifth transport pump 14 for centrifugation;
  • Step 3-2 centrifugal separation: some insoluble gas mixed with the salt solution sent to the centrifuge 15 is discharged through the thirteenth one-way valve V30 above the centrifuge 15. After the remaining solid-liquid mixture is centrifuged, the solid salt block is stored. It is stored in the salt tank 16 as the raw material for subsequent deep processing, and the remaining incompletely centrifuged solution flows back into the salt solution tank 13 through the liquid phase outlet of the centrifuge, which not only replenishes the liquid level of the salt solution tank 13, but also participates in the centrifugal reduction. loss;
  • Step 3-3 water injection: once the salt solution in the salt solution tank 13 meets the centrifugal requirements, the continuous centrifugation will cause the liquid level in the tank to drop continuously, which may endanger the stability of the entire system.
  • the second liquid level controller S36 sends a signal to control the system to open the fourth electric valve V22 to extract water from the water tank 11 and inject it into the salt solution tank 13 , to ensure the stability of the liquid level in the salt solution tank 13; at the same time, water injection will also reduce the solution salt concentration in the salt solution tank 13, when the second conductivity measuring instrument S38 measures the salt solution in the solution tank 13
  • the concentration of salt in the tank 13 is lower than the set value Afterwards, stop the operation of the centrifuge 15, and close the fifth electric valve V27 and the fifth transport pump 14, until the next centrifugation processing condition is satisfied, and then go to step 3-1 for circulation.
  • the liquid level in the negative pressure flash tank 3 is set through the liquid level transmitter to set the liquid level limit high alarm, liquid level high alarm, liquid level low alarm and liquid level limit low alarm, when the liquid level is not within the normal range
  • the following methods are used to deal with it:
  • the high liquid level limit alarm is triggered, and the first electric valve V4 in the feeding circuit is cut off to prevent the salt-containing ethylene glycol from being lean.
  • the liquid is immersed in the mist eliminator or into the condenser; after that, as the distillation process continues, the liquid level in the negative pressure flash tank 3 drops below 550mm, and when the low liquid level alarm is triggered, the feed is turned on again.
  • the circulating heater 5 is shut down urgently to control the temperature of the salt-containing ethylene glycol lean liquid in the negative pressure flash tank 3. Below 170°C; after that, the salt-containing ethylene glycol lean liquid newly injected into the negative pressure flash tank 3 has a slow distillation process due to insufficient heating, and the liquid level in the negative pressure flash tank 3 will gradually increase.
  • the high liquid level alarm is triggered, and the circulating heater 5 is restarted; the liquid level in the negative pressure flash tank 3 is prevented from being lower than the circulating outlet pipeline, and a protection mechanism is formed, which improves the safety and stability of the system. sex.
  • the high liquid level alarm is triggered.
  • the circulating heater 5 is activated and its heating value is 160°C, the upper limit of the working temperature.
  • the upper limit of the working temperature is 160°C
  • the circulating heater 5 is operated according to the heating value of the upper limit of the working temperature of 160°C, so as to speed up the distillation speed of the salt-containing ethylene glycol lean liquid in the negative pressure flash tank 3; if this
  • the opening of the first flow control valve V5 in the feeding loop is reduced to reduce the feeding speed;
  • the low liquid level alarm is triggered, and the opening of the first flow control valve V5 in the feed circuit is adjusted to the maximum; if the feed flow has reached the maximum, the circulation is reduced.
  • the working temperature of the heater 5 is set to the set working temperature value of 140-150°C, thereby reducing the distillation speed.
  • the pressure transmitter on the upper part of the negative pressure flash tank 3 is set with high pressure alarm, low pressure alarm and high pressure limit alarm.
  • the corresponding alarm is triggered , which is processed as follows:
  • the working temperature of the circulating heater 5 is reduced to the set working temperature value of 140°C, and the first flow control valve V5 is adjusted. The opening is adjusted to the minimum;
  • the temperature transmitter in the negative pressure flash tank 3 is set with low temperature alarm, high temperature alarm, and high temperature limit alarm. When the temperature in the negative pressure flash tank 3 is not within the normal range, the corresponding alarm is triggered , proceed as follows:
  • the circulating heater 5 When the temperature in the negative pressure flash tank 3 is lower than 120°C and the low temperature alarm is triggered, the circulating heater 5 is adjusted to work under the condition that the heating value is the upper limit of the set working temperature of 160°C, so that the flashing The solution in the steaming tank is heated up to the set normal range of 140-150°C as soon as possible; if the circulating heater 5 has been operated under the condition that the heating value is the upper limit of the set working temperature of 160°C, the first temperature on the feeding loop will be reduced.
  • the opening of the flow control valve V5 reduces the feed flow to 15 m 3 /h; the temperature in the negative pressure flash tank 3 is monitored in real time, and the temperature is supplemented in time when the temperature drops, which ensures the full progress of the flash and improves the The efficiency of flash separation improves the product quality of the MEG lean liquid recovered in the system.
  • the circulating heater 5 When the temperature in the negative pressure flash tank 3 is higher than 170°C, and an alarm of excessive temperature limit is triggered, the circulating heater 5 is turned off immediately, and the operator is waiting for intervention. Effectively prevent the thermal decomposition of ethylene glycol because the temperature exceeds the thermal decomposition temperature, and improve the recovery rate of the ethylene glycol lean liquid in the system.
  • the circulating heater 5 When the density of the MEG lean liquid measured in real time by the density indicator in the MEG lean liquid receiving tank 7 is less than the set lower limit value of 1.03 ⁇ 10 3 kg/m 3 , check whether the circulating heater 5 is activated and its heating value is set to The upper limit of the working temperature is set to 160°C. If it is not started or the heating value does not reach the upper limit of the set working temperature of 160°C, the circulating heater 5 will be heated up to the upper limit of the set working temperature of 160°C to speed up the operation.
  • the circulating heater 5 When the density of the MEG lean liquid in the MEG lean liquid receiving tank 7 measured in real time is less than the qualified value 1.1 ⁇ 10 3 kg/m 3 , check whether the circulating heater 5 is activated and its heating value is the set working temperature The upper limit value is 160°C. If it is not started or the heating value does not reach the set working temperature upper limit value of 160°C, make the circulating heater 5 work according to the heating value of the set working temperature upper limit value of 160°C to speed up the negative pressure.
  • the opening of the first flow control valve V5 in the feed circuit is to reduce the feed rate drop and improve the separation efficiency of the negative pressure flash tank 3;

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Abstract

一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统及其脱盐方法，脱盐系统包括MEG贫液回收装置、含盐乙二醇贫液闪蒸装置以及一阶盐回收装置；含盐乙二醇贫液闪蒸装置包括含盐乙二醇贫液罐（1）、第一运输泵（2）、负压闪蒸罐（3）、第二运输泵（4）、循环加热器（5）；MEG贫液回收装置包括负压冷凝器（6）、MEG贫液接收罐（7）、真空泵（8）、第三运输泵（9）、合格MEG贫液存储罐（10）；一阶盐回收装置包括水罐（11）、第四运输泵（12）、盐液罐（13）、第五运输泵（14）、离心机（15）、盐罐（16）。

Description

深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统及其脱盐方法 技术领域
本发明涉及一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统及其脱盐方法。
背景技术
在深水天然气田开采中，由于水下温度和压力的变化会形成天然气水合物，造成系统设备和管线的堵塞，乙二醇因其挥发性低、易与水分离的特点，常用作为水合物抑制剂来防止管道和设备的堵塞，为了降低成本需要借助乙二醇再生与回收系统(MRU)来实现乙二醇的循环利用。
从管道中回流的乙二醇溶液在吸收了部分采出液后，通常都含有一定量的盐类。传统的乙二醇回收技术难以脱除乙二醇中的盐类，当含盐较多时，再生回收乙二醇时盐易在再生流程中沉积在容器内表面，出现结垢现象，堵塞管道，导致整个流程无法正常工作。
深水气田开发中采出液含盐量高，现有手段不足以脱除其中盐分；陆上气田开发中也存在同样的问题，如新疆克拉美丽气田产出水中含盐量高，而乙二醇再生系统未进行脱盐处理，导致重沸器内结垢堵塞。
发明内容
本发明所要解决的技术问题是：提供一种能够高效去除乙二醇贫液中高溶解度盐离子的脱盐系统。
为解决上述技术问题，本发明所采用的技术方案为：一种深海天然气开采中含高溶解度盐乙二醇贫液的脱盐系统，包括MEG贫液回收装置、含盐乙二醇贫液闪蒸装置以及一阶盐回收装置；
其中，含盐乙二醇贫液闪蒸装置包含含盐乙二醇贫液罐，其通过管道与第一运输泵连接，在含盐乙二醇贫液罐与第一运输泵之间的管道上安装有第一截止阀，第一运输泵通过管道与负压闪蒸罐相连接，在第一运输泵至负压闪蒸罐之间的管道上依次安设有第一单向阀、第一电动阀和第一流量控制阀，在第一运输泵和单向阀之间的管道上安设有第一温度变送器，在电动阀和流量控制阀之间的管道上安设有第一流量变送器和第一流量控制仪，负压闪蒸罐设有两个液相出口和一个位于罐顶的气相出口，气相出口通过管道连通负压冷凝器，其中一个液相出口通过降液管连接盐液罐，另一个液相出口通过第二运输泵连接循 环加热器并且循环加热器的出口连接负压闪蒸罐形成闭环回路；
在负压闪蒸罐上安设有实时监控并控制负压闪蒸罐内的压力的第一压力控制器、第二压力变送器和第一压力表，负压闪蒸罐上还安设有温度表和温度校验仪，在负压闪蒸罐和第二运输泵之间的管路上安设有第四压力变送器和第五单向阀，在第二运输泵和循环加热器之间的管路上安设有第六单向阀和第七单向阀，在第六单向阀和第七单向阀之间的管路上布置有第五压力变送器和第三温度表；循环加热器的出口通过设置第八单向阀的管道和负压闪蒸罐连接，在第八单向阀和负压闪蒸罐之间的管道上安设有用以确保经加热后的MEG贫液温度与达到指定值的第二压力控制器、第四温度表、第四温度变送器和第五温度表；
含盐乙二醇贫液闪蒸装置包括通过设置第二单向阀的管道和负压闪蒸罐连通的负压冷凝器，负压闪蒸罐与负压冷凝器两者之间的管道上安设有第一压差变送器、第二压力表和第二温度变送器；负压冷凝器通过设有第三单向阀和第二电动阀的管道连接MEG贫液接收罐，管道上在负压冷凝器和第三单向阀之间安设有第三压力表，在第二电动阀和MEG贫液接收罐之间的管道上布置有用以确认闪蒸后获得的MEG贫液之中的高溶解度一价盐离子含量的第一电导率测定仪、以及第三温度变送器和温度控制器；MEG贫液接收罐上设有第三压力变送器、第二温度表和液位仪；MEG贫液接收罐顶部设有一气相出口通过设有真空阀的管道连接真空泵，MEG贫液接收罐底部的液相出口通过第三截止阀连接第三运输泵，在第三截止阀的入口和第三运输泵的出口之间连接有第二旁通阀，第三运输泵通过第四单向阀与合格MEG贫液存储罐连通；
一价盐回收系统包含有水罐，水罐通过设置第四运输泵的管道与盐液罐连通，在第四运输泵的出口至盐液罐之间的管道上依次安设有第十单向阀、第四电动阀和第二流量控制阀；在第四运输泵和单向阀之间的管道上设有第四压表，在电动阀和流量控制阀之间的管道上安设有根据盐液罐中盐溶液浓度控制进水量大小的第二流量变送器和第二流量控制仪；负压闪蒸罐至盐液罐之间通过依次设有第九单向阀和第三电动阀的管道相连接，盐液罐上布置有用以实时监控盐液罐内的盐溶液浓度并维持盐液罐内液面稳定的第七温度表、第二液位变送器、第二液位控制器、第五压力表和第二电导率测定仪；
盐液罐通过两条并列布置的设置第五截止阀的管道和第五旁通阀的管道分别与第五运输泵相连，第五运输泵和离心机之间的管道上连接有第十一单向阀和第五电动阀，运输泵和单向阀之间的管道上设有第六压力变送器，第五电动阀和离心机之间的管道上设有第三流量变送器和第三流量控制器；离心机上设有位于顶部的气相出口、位于底部的固相出口， 其中位于顶部的气相出口通过设置第十三单向阀的管道与外界连通，位于底部的固相出口通过设置第十四单向阀的管道与盐罐连通。
作为一种优选的方案，在第一运输泵的输出口还通过设置第一旁通阀的管道连接至含盐乙二醇贫液罐和第一截止阀之间的管道上形成第一旁通回路，在第一旁通回路的回路连接口与第一截止阀之间的管道上安装有第一压力变送器。
作为一种优选的方案，所述负压闪蒸罐的罐体内侧下部设有控制最低液位以保证罐内闪蒸的MEG贫液量的稳定的第一液位变送器和第一液位控制器。
作为一种优选的方案，所述第六单向阀出口端的管道和第七单向阀出口端的管道间连接有第二压差变送器。
作为一种优选的方案，所述第四运输泵通过设置第四截止阀和第四旁通阀的管道构成旁通回路。
作为一种优选的方案，所述离心机上设有位于底部循环回路出口，循环回路出口通过设置第十二单向阀和第六电动阀的管道与盐液罐连接。
本系统的有益效果是：
本系统高效的实现了用于深海天然气开采的含盐乙二醇贫液的脱盐回收与再利用，并且极大程度上减少了乙二醇的损失，以降低使用成本；将含盐乙二醇贫液中的一价盐NACL晶体提取出来，可用作于后续的深加工，提高了经济效益。
由于在电动阀和流量控制阀之间的管道上安设有第一流量变送器和第一流量控制仪，可根据负压负压闪蒸罐内的压力、液面、温度等信息，调节运输管内的流量大小；由于负压闪蒸罐的罐体内侧下部设有控制最低液位以保证罐内闪蒸的MEG贫液量的稳定的第一液位变送器和第一液位控制器；由于在第八单向阀和负压闪蒸罐之间的管道上安设有第二压力控制器、第四温度表、第四温度变送器和第五温度表，可以确保经加热后的MEG贫液温度与达到指定值。由于MEG贫液接收罐上设有第三压力变送器、第二温度表和液位仪，可以监测罐内的压力、温度与液位。由于盐液罐上布置有第七温度表、第二液位变送器、第二液位控制器、第五压力表和第二电导率测定仪，可以实时监控盐液罐内的盐溶液浓度并维持盐液罐内液面稳定。
本系统中的料液运输均采用了旁通回路的方式，可以保证管道在运输溶液过程中的稳定性，提高整个系统的安全性。
本发明所要解决的另一个技术问题是：提供一种上述深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法。
为解决上述技术问题，本发明所采用的技术方案为：深海天然气开采含高溶解度盐乙二醇贫液的脱盐系统的脱盐方法，具体过程如下：
步骤1，含盐乙二醇贫液闪蒸：
步骤1-1，原料运输：初始状态时，各个系统中的阀门均处于关闭状态；首先打开第一截止阀和第一旁通阀，启动第一运输泵，当含盐乙二醇贫液罐和第一运输泵之间的旁通回路充满MEG贫液后，第一压力变送器检测到管内压力稳定，然后通过远程控制打开电动阀，并且打开第一流量控制阀，同时关闭第一旁通阀，将含盐乙二醇贫液原料运送至负压闪蒸罐内；
步骤1-2，流量控制：当负压闪蒸罐上的第一液位变送器检测到罐内溶液达到指定液位后，通过控制系统控制进料管上的第一流量控制阀，调整罐内流量大小，维持负压闪蒸罐的液位平稳；若突遇紧急状况，则直接远程关闭第一电动阀，阻止原料的流入；
步骤1-3，循环加热：流入负压闪蒸罐内的含盐乙二醇贫液，通过第二运输泵转送至循环加热器中加热并重新流回至负压闪蒸罐内，位于负压闪蒸罐上的温度校验仪和第四温度变送器实时监控罐内温度，确保罐内温度稳定在140±5℃；
步骤1-4，闪蒸：负压闪蒸罐上的第一压力控制器和第二压力变送器确保负压闪蒸罐的操作压力保持在15±5KPa；由于压力的下降，负压闪蒸罐内的乙二醇开始进行闪蒸分离，通过循环加热回路进行温度补充，来维持闪蒸过程中所需的温度，MEG贫液被蒸馏出来并以气相形式堆积在负压闪蒸罐的顶部；
步骤2，MEG贫液回收：
步骤2-1，MEG贫液冷凝：经由闪蒸产生的MEG贫液气体经过第二单向阀进入负压冷凝器中，使热蒸汽迅速降温至40±3℃使得MEG贫液气体重新液化，然后打开第二电动阀，将冷凝液汇入MEG贫液接收罐；
步骤2-2，提纯：打开真空阀、气动真空泵，将MEG贫液接收罐中的少量气体排出，剩余的MEG贫液则通过第三运输泵存储到合格MEG贫液存储罐中；
步骤3，一价盐回收：
步骤3-1，盐液存储：由步骤1-4中得到的位于负压闪蒸罐底部的盐溶液通过降液管被运送至盐液罐中，盐液罐中的一价盐已经达到饱和状态，开始结晶析出，待第二电导率测定仪测得盐液罐中盐浓度达到设定值后，通过第五运输泵运送至离心机中离心；
步骤3-2，离心分离：送往离心机中的盐液内混杂一些不溶气体通过离心机上方的第十三单向阀排出，剩余固液混合物经离心后，固体盐块被存入盐罐中进行保存作为后续深加 工原料，剩余未完全离心的溶液则通过离心机的液相出口重新回流入盐液罐中；
步骤3-3，注水：当第二液位变送器检测盐液罐中的液面下降至下限值时，第二液位控制器则发出信号，控制系统开启第四电动阀，从水罐中抽取水注入盐液罐中，保证盐液罐中液面的稳定；当第二电导率测定仪测得盐液罐中盐浓度低于设定值后，停止离心机的工作，并关闭第五电动阀和第五运输泵，直至下一个离心处理条件满足，转至步骤3-1进行循环。
作为一种优选的方案，所述负压闪蒸罐内的液位通过液位变送器设置了液位极限过高报警、液位过高报警、液位过低报警以及液位极限过低报警，当液位不在正常范围内，导致触发了以上报警时，按照如下方式进行处理：
当负压闪蒸罐内含盐乙二醇贫液液位过高触发了液位极限过高报警，则切断进料回路中的第一电动阀以防止含盐乙二醇贫液浸没除雾器或进入到冷凝器中；此后，随着蒸馏过程的继续，负压闪蒸罐内的液位降低至触发液位过低报警时，再重新打开进料回路；
当负压闪蒸罐内液面高度过低触发了液位极限过低报警，则紧急关闭循环加热器以将负压闪蒸罐内含盐乙二醇贫液的温度控制在170℃以下；此后，新注入到负压闪蒸罐内的含盐乙二醇贫液由于加热不足导致其蒸馏进程缓慢，负压闪蒸罐内的液位将逐步升高，当液位过高导致触发液位过高报警时，再重新启动循环加热器；
当负压闪蒸罐内液面过高触发了液位过高报警，检查循环加热器是否启动且其加热值为工作温度上限值，若未启动或加热值未达工作温度上限值，则使循环加热器按加热值为工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到工作温度上限值，则减小进料回路中第一流量控制阀的开度以将降低进料速度；
过负压闪蒸罐内液位过低触发了液位过低报警，调整进料回路中的第一流量控制阀开度至最大；若进料流量已至最大，则降低循环加热器的工作温度至设定工作温度值，从而降低蒸馏速度。
作为一种优选的方案，所述负压闪蒸罐上部的压力变送器设置了压力过高报警、压力过低报警以及压力极限过高报警，当负压闪蒸罐内压力不在正常范围内，导致触发了相应报警时，按照如下方式进行处理：
当负压闪蒸罐工作温度上限值内压力过低导致触发了压力过低报警时，则增大循环加热器的工作温度至工作温度上限值；
当负压闪蒸罐内压力过高导致触发了压力过高报警时，则减小循环加热器的工作温度 至设定工作温度值，调节第一流量控制阀的开度调至最小；
当负压闪蒸罐内压力超高触发了压力极限过高报警时，关闭第一电动阀从而切断进料，关闭循环加热器，等待操作人员介入处理。
作为一种优选的方案，所述负压闪蒸罐内的温度变送器设置了温度过低报警、温度过高报警、温度极限过高报警，当负压闪蒸罐中的温度不在正常范围内，导致触发了相应报警时，按照如下的方式进行处理：
当负压闪蒸罐内的温度低于120℃，触发了温度过低报警时，将循环加热器调整在加热值为设定工作温度上限值的情形下工作，以使得负压闪蒸罐内的溶液尽快升温到设定正常范围；若循环加热器已在加热值为设定工作温度上限值的情形下工作，则减小进料回路上第一流量控制阀的开度使进料流量降低；
当负压闪蒸罐内的温度过高触发了温度过高报警时，则降低循环加热器的工作温度至设定工作温度值；
当负压闪蒸罐内的温度超高触发了温度极限过高报警时，立即关闭循环加热器，等待操作人员介入处理。
作为一种优选的方案，当MEG贫液接收罐内的密度指示器进行实时测量的MEG贫液的密度小于设定下限值时，检查循环加热器是否启动且其加热值为设定工作温度上限值，若未启动或加热值未达设定工作温度上限值，则使循环加热器升温至按设定工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到设定工作温度上限值，则减小进料回路中第一流量控制阀的开度开到最小，或将进料回路上的第一流量控制阀关闭，待乙二醇纯度达到预设值，再重新打开第一电动阀，将第一流量控制阀的开度开到正常值，降低循环加热器的加热温度至设定工作温度值；
当MEG贫液接收罐内的MEG贫液的密度指示器进行实时测量的密度小于合格值时，检查循环加热器是否启动且其加热值为设定工作温度上限值，若未启动或加热值未达设定工作温度上限值，则使循环加热器按加热值为设定工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到设定工作温度上限值，则减小进料回路中第一流量控制阀的开度以降低进料速度降，提高负压闪蒸罐的分离效率。
本方法的有益效果是：本方法可使得脱盐系统完成对深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐操作，且乙二醇回收利用率高，操作安全可靠。
在步骤1-1原料运输中，打开第一流量控制阀，同时关闭第一旁通阀，以将约95℃含盐乙二醇贫液原料运送至负压闪蒸罐内，可防止直接打开阀门运输对机构造成冲击；
在步骤2-2提纯中，由于MEG贫液气体在冷凝过程中难免会夹杂有少量不冷凝气体，跟随冷凝液一同汇入MEG贫液接收罐中，因此打开真空阀、气动真空泵，将MEG贫液接收罐中的少量气体排出；
在步骤3-2离心分离中，送往离心机中的盐液内混杂一些不溶气体通过离心机上方的第十三单向阀排出，剩余固液混合物经离心后，固体盐块被存入盐罐中进行保存作为后续深加工原料，剩余未完全离心的溶液则通过离心机的液相出口重新回流入盐液罐中，不仅补充盐液罐的液位，也重新参与离心以减少乙二醇损失；
在步骤3-3中，由于盐液罐中的盐液一旦满足离心要求，则不断进行离心导致罐内液面的不断下降，从而可能危害整个系统的稳定，所以当第二液位变送器检测盐液罐中的液面下降至下限值时，第二液位控制器则发出信号，控制系统开启第四电动阀，从水罐中抽取水注入盐液罐中，保证盐液罐中液面的稳定；同时注水也会使得盐液罐中的溶液盐浓度降低。
在步骤1-4中，负压闪蒸罐上的第一压力控制器和第二压力变送器确保负压闪蒸罐的操作压力保持在15±5KPa；当负压闪蒸罐内的压力和温度均达到设定值后，一价盐在乙二醇液中达到饱和状态，含盐乙二醇贫液开始进行闪蒸分离，通过循环加热回路进行温度补充，来维持闪蒸过程中所需的温度，MEG贫液被蒸馏出来并以气相形式堆积在负压闪蒸罐的顶部，提高了闪蒸脱盐的效率。
如果负压闪蒸罐内液位过高，溶液有可能会浸没安装在负压闪蒸罐顶部的除雾器，将其腐蚀导致其不能正常工作；若液位过低，表示负压闪蒸罐内含盐乙二醇贫液不足，这将影响实验装置中其它设备的正常工作，导致实验系统整体运行效率低下，影响实验结果。本方法有效实现了负压闪蒸罐内液位控制。
当负压闪蒸罐中的液位处于正常水平时，应判断其中的压力水平是否正常。从而保证相关仪器设备的正常工作环境，提高含盐乙二醇贫液的蒸馏效率。
当负压闪蒸罐中的液位、压力均处于正常水平时，应判断其中的温度水平是否正常。从而进一步保证相关仪器设备的正常工作环境，提高含盐乙二醇贫液的蒸馏效率。
MEG贫液接收罐罐内的乙二醇的纯度不够会导致产品不合格，达不到生产的要求，会对整个乙二醇再生与回收系统造成经济损失。当脱盐装置启动后，随着负压闪蒸罐中气液分离过程的不断进行，脱盐后的MEG贫液的不断的产出并收集到MEG贫液接收罐中，随 着MEG贫液接收罐内的液位不断升高，待液位高度达到预先设置的控制点，通过第三运输泵将脱盐后的MEG贫液抽出，MEG贫液接收罐罐中液体密度通过安装在回路中的密度指示器进行实时测量。当测得的密度未达到预先设定的限值时，将控制进料回路上的流量的大小以及循环加热器的工作温度来进行控制，从而保证MEG贫液接收罐罐内的乙二醇的纯度合格。
附图说明
图1是本发明的脱盐系统布置图。
图1中：1-含盐乙二醇贫液罐，2-第一运输泵，3-负压闪蒸罐，4-第二运输泵，5-循环加热器，6-负压冷凝器，7-MEG贫液接收罐，8-真空泵，9-第三运输泵，10-合格MEG贫液存储罐，11-水罐，12-第四运输泵，13-盐液罐，14-第五运输泵，15-离心机，16-盐罐；
V1-第一截止阀，V2-第一旁通阀，V3-第一单向阀，V4-第一电动阀，V5-第一流量控制阀，V6-第二单向阀，V7-第三单向阀，V8-第二电动阀，V9-真空阀，V10-第三截止阀，V11-第二旁通阀，V12-第四单向阀，V13-第五单向阀，V14-第六单向阀，V15-第七单向阀，V16-第八单向阀，V17-第九单向阀，V18-第三电动阀，V19-第四截止阀，V20-第四旁通阀，V21-第十单向阀，V22-第四电动阀，V23-第二流量控制阀，V24-第五截止阀，V25-第五旁通阀，V26-第十一单向阀，V27-第五电动阀，V28-第十二单向阀，V29-第六电动阀，V30-第十三单向阀，V31-第十四单向阀；
S1-第一压力变送器，S2-第一温度变送器，S3-第一流量变送器，S4-第一流量控制仪，S5-第一压力控制器，S6-第二压力变送器，S7-第一压力表，S8-第一液位变送器，S9-第一液位控制器，S10-第一温度表，S11-温度校验仪，S12-第一压差变送器，S13-第二温度变送器，S14-第二压力表，S15-第三压力表，S16-第一电导率测定仪，S17-第三温度变送器，S18-温度控制器，S19-第三压力变送器，S20-第二温度表，S21-液位仪，S22-第四压力变送器，S23-第五压力变送器，S24-第三温度表，S25-第二压差变送器，S26-第二压力控制器，S27-第四温度表，S28-第四温度变送器，S29-第五温度表，S30-第六温度表，S31-第四压力表，S32-第二流量变送器，S33-第二流量控制仪，S34-第七温度表，S35-第二液位变送器，S36-第二液位控制器，S37-第五压力表，S38-第二电导率测定仪，S39-第六压力变送器，S40-第三流量变送器，S41-第三流量控制器。
具体实施方式
下面结合附图，详细描述本发明的具体实施方案。
如图1所示，一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，包括MEG 贫液回收装置、含盐乙二醇贫液闪蒸装置以及一阶盐回收装置；
其中，含盐乙二醇贫液闪蒸装置包含含盐乙二醇贫液罐1，其通过管道与第一运输泵2连接，在含盐乙二醇贫液罐1与第一运输泵2之间的管道上安装有第一截止阀V1，在第一运输泵2的输出口连接有三通阀，三通阀的其中一路通过设置第一旁通阀V2的管道连接至含盐乙二醇贫液罐和第一截止阀V1之间的管道上形成第一旁通回路，在第一旁通回路的回路连接口与第一截止阀V1之间的管道上安装有第一压力变送器S1；第一运输泵2通过管道与负压闪蒸罐3相连接，在第一运输泵2至负压闪蒸罐3之间的管道上依次安设有第一单向阀V3、第一电动阀V4和第一流量控制阀V5，在第一运输泵2和单向阀V3之间的管道上安设有第一温度变送器S2，在电动阀V4和流量控制阀V5之间的管道上安设有第一流量变送器S3和第一流量控制仪S4，可根据负压负压闪蒸罐3内的压力、液面、温度等信息，调节运输管内的流量大小；负压闪蒸罐设有两个液相出口和一个位于罐顶的气相出口，气相出口通过管道连通负压冷凝器6，其中一个液相出口通过降液管连接盐液罐13，另一个液相出口通过第二运输泵4连接循环加热器5并且循环加热器5的出口连接负压闪蒸罐3形成闭环回路；
在负压闪蒸罐3上安设有实时监控并控制负压闪蒸罐3内的压力的第一压力控制器S5、第二压力变送器S6和第一压力表S7，负压闪蒸罐3上还安设有温度表S10和温度校验仪S11，负压闪蒸罐3的罐体内侧下部设有控制最低液位以保证罐内闪蒸的MEG贫液量的稳定的第一液位变送器S8和第一液位控制器S9；在负压闪蒸罐3和第二运输泵4之间的管路上安设有第四压力变送器S22和第五单向阀V13，在第二运输泵4和循环加热器5之间的管路上安设有第六单向阀V14和第七单向阀V15，在第六单向阀V14和第七单向阀V15之间的管路上布置有第五压力变送器S23和第三温度表S24；循环加热器5的出口通过设置第八单向阀V16的管道和负压闪蒸罐3连接，第六单向阀V14出口端的管道和第七单向阀V15出口端的管道间连接有第二压差变送器S25，在第八单向阀V16和负压闪蒸罐3之间的管道上安设有用以确保经加热后的MEG贫液温度与达到指定值的第二压力控制器S26、第四温度表S27、第四温度变送器S28和第五温度表S29。
MEG回收系统包括通过设置第二单向阀V6的管道和负压闪蒸罐3连通的负压冷凝器6，负压闪蒸罐3与负压冷凝器6两者之间的管道上安设有第一压差变送器S12、第二压力表S14和第二温度变送器S13；负压冷凝器6通过设有第三单向阀V7和第二电动阀V8的管道连接MEG贫液接收罐7，管道上在负压冷凝器6和第三单向阀V7之间安设有第三压力表S15，在第二电动阀V8和MEG贫液接收罐7之间的管道上布置有用以确认闪蒸后获 得的MEG贫液之中的高溶解度一价盐离子含量的第一电导率测定仪S16、以及第三温度变送器S17和温度控制器S18；MEG贫液接收罐7上设有第三压力变送器S19、第二温度表S20和液位仪S21，用以监测罐内的压力、温度与液位；MEG贫液接收罐7顶部设有一气相出口通过设有真空阀V9的管道连接真空泵8，MEG贫液接收罐7底部的液相出口通过第三截止阀V10连接第三运输泵9，在第三截止阀V10的入口和第三运输泵9的出口之间连接有第二旁通阀V11，第三运输泵9通过第四单向阀V12与合格MEG贫液存储罐10连通。
一价盐回收系统包含有水罐11，水罐11通过设置第四运输泵12的管道与盐液罐13连通，第四运输泵12通过设置第四截止阀V19和第四旁通阀V20的管道构成旁通回路；在第四运输泵12的出口至盐液罐13之间的管道上依次安设有第十单向阀V21、第四电动阀V22和第二流量控制阀V23；在第四运输泵12和单向阀V21之间的管道上设有第四压表S31，在电动阀V22和流量控制阀V23之间的管道上安设有根据盐液罐13中盐溶液浓度控制进水量大小的第二流量变送器S32和第二流量控制仪S33；负压闪蒸罐3至盐液罐13之间通过依次设有第九单向阀V17和第三电动阀V18的管道相连接，盐液罐13上布置有用以实时监控盐液罐13内的盐溶液浓度并维持盐液罐13内液面稳定的第七温度表S34、第二液位变送器S35、第二液位控制器S36、第五压力表S37和第二电导率测定仪S38；
罐13通过两条并列布置的设置第五截止阀V24的管道和第五旁通阀V25的管道与第五运输泵14相连，第五运输泵14和离心机15之间的管道上连接有第十一单向阀V26和第五电动阀V27，运输泵14和单向阀V26之间的管道上设有第六压力变送器S39，第五电动阀V27和离心机15之间的管道上设有第三流量变送器S40和第三流量控制器S41；离心机15上设有位于顶部的气相出口、位于底部的固相出口以及循环回路出口，其中位于顶部的气相出口通过设置第十三单向阀V30的管道与外界连通，位于底部的固相出口通过设置第十四单向阀V31的管道与盐罐16连通，循环回路出口通过设置第十二单向阀V28和第六电动阀V29的管道与盐液罐13连接。
深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，具体如下：
步骤1，含盐乙二醇贫液闪蒸：
步骤1-1，原料运输：初始状态时，各个系统中的阀门均处于关闭状态；首先打开第一截止阀V1和第一旁通阀V2，启动第一运输泵2，当含盐乙二醇贫液罐1和第一运输泵2之间的旁通回路充满MEG贫液后，第一压力变送器S1检测到管内压力稳定，然后通过远程控制打开电动阀V4，并且打开第一流量控制阀V5，同时关闭第一旁通阀V2，将约95℃ 含盐乙二醇贫液原料运送至负压闪蒸罐3内，可防止直接打开阀门运输对机构造成冲击；
步骤1-2，流量控制：当负压闪蒸罐3上的第一液位变送器S8检测到罐内溶液达到指定液位后，通过控制系统控制进料管上的第一流量控制阀V5，调整罐内流量大小，维持负压闪蒸罐3的液位平稳；若突遇紧急状况，则直接远程关闭第一电动阀V4，阻止原料的流入；
步骤1-3，循环加热：95℃含盐贫乙二醇料液在负压闪蒸罐无法达到闪蒸的要求，因此需对其进行加热。流入负压闪蒸罐3内的含盐乙二醇贫液，通过第二运输泵4转送至循环加热器5中加热并重新流回至负压闪蒸罐3内，位于负压闪蒸罐3上的温度校验仪S11和第四温度变送器S28实时监控罐内温度，确保罐内温度稳定在140±5℃；
步骤1-4，闪蒸：闪蒸不仅需要温度达到一定值，对压力也有所要求，负压闪蒸罐上的第一压力控制器S5和第二压力变送器S6确保负压闪蒸罐的操作压力保持在15±5KPa；当负压闪蒸罐内的压力和温度均达到设定值后，一价盐NaCl在乙二醇液中达到饱和状态，含盐乙二醇贫液开始闪蒸，经过不断的循环加热，MEG贫液被蒸馏出来并以气相形式堆积在负压闪蒸罐3的顶部，剩余的负压闪蒸罐3底部的溶液90％以上为含一价盐溶液；
步骤2，MEG贫液回收：
步骤2-1，MEG贫液冷凝：经由闪蒸产生的MEG贫液气体经过第二单向阀V6进入负压冷凝器中，使热蒸汽迅速降温至40±3℃使得MEG贫液气体重新液化，然后打开第二电动阀V8，将冷凝液汇入MEG贫液接收罐7；
步骤2-2，提纯：由于MEG贫液气体在冷凝过程中难免会夹杂有少量不冷凝气体，跟随冷凝液一同汇入MEG贫液接收罐中，因此打开真空阀V9、气动真空泵9，将MEG贫液接收罐中的少量气体排出，剩余的MEG贫液则通过第三运输泵9存储到合格MEG贫液存储罐10中，重新作为海洋天然开发过程中用的抑制剂；
步骤3，一价盐回收：
步骤3-1，盐液存储：由步骤1-4中得到的位于负压闪蒸罐3底部的盐溶液通过降液管被运送至盐液罐13中，盐液罐13中的一价盐如NaCl等已经达到饱和状态，开始结晶析出，待第二电导率测定仪S38测得盐液罐13中盐浓度达到设定值后，通过第五运输泵14运送至离心机15中离心；
步骤3-2，离心分离：送往离心机15中的盐液内混杂一些不溶气体通过离心机15上方的第十三单向阀V30排出，剩余固液混合物经离心后，固体盐块被存入盐罐16中进行保存作为后续深加工原料，剩余未完全离心的溶液则通过离心机的液相出口重新回流入盐液罐 13中，不仅补充盐液罐13的液位，也重新参与离心减少损失；
步骤3-3，注水：由于盐液罐13中的盐液一旦满足离心要求，则不断进行离心导致罐内液面的不断下降，从而可能危害整个系统的稳定，当第二液位变送器S35检测盐液罐13中的液面下降至下限值时，第二液位控制器S36则发出信号，控制系统开启第四电动阀V22，从水罐11中抽取水注入盐液罐13中，保证盐液罐13中液面的稳定；同时注水也会使得盐液罐13中的溶液盐浓度降低，当第二电导率测定仪S38测得盐液罐13中盐浓度低于设定值后，停止离心机15的工作，并关闭第五电动阀V27和第五运输泵14，直至下一个离心处理条件满足，转至步骤3-1进行循环。
负压闪蒸罐3内的液位通过液位变送器设置了液位极限过高报警、液位过高报警、液位过低报警以及液位极限过低报警，当液位不在正常范围内，导致触发了以上报警时，按照如下方式进行处理：
当负压闪蒸罐3内含盐乙二醇贫液液位高于1450mm，触发了液位极限过高报警，则切断进料回路中的第一电动阀V4以防止含盐乙二醇贫液浸没除雾器或进入到冷凝器中；此后，随着蒸馏过程的继续，负压闪蒸罐3内的液位降低至低于550mm，触发液位过低报警时，再重新打开进料回路；有效防止负压闪蒸罐3内含盐MEG贫液浸没除雾器或进入到冷凝器中，避免了设备被腐蚀，提高了系统设备的安全性，降低了设备损坏的风险和设备的更换周期。
当负压闪蒸罐3内液面高度低于550mm，触发了液位极限过低报警，则紧急关闭循环加热器5以将负压闪蒸罐3内含盐乙二醇贫液的温度控制在170℃以下；此后，新注入到负压闪蒸罐3内的含盐乙二醇贫液由于加热不足导致其蒸馏进程缓慢，负压闪蒸罐3内的液位将逐步升高，当液位过高导致触发液位过高报警时，再重新启动循环加热器5；防止负压闪蒸罐3内液位低于循环出口管线，形成了保护机制，提高了系统的安全性和稳定性。
当负压闪蒸罐3内液面高于1100mm，触发了液位过高报警，检查循环加热器5是否启动且其加热值为工作温度上限值160℃，若未启动或加热值未达工作温度上限值160℃，则使循环加热器5按加热值为工作温度上限值160℃进行工作，以加快负压闪蒸罐3内含盐乙二醇贫液的蒸馏速度；若此时循环加热器5已经启动，且此时循环加热器5的加热量达到工作温度上限值160℃，则减小进料回路中第一流量控制阀V5的开度以将降低进料速度；通过实时监测和调节负压闪蒸罐3内的液位水平，保证进料流量的动态平衡，提高了负压闪蒸罐3内的分离效率，降低系统能耗。
当负压闪蒸罐3内液位低于700mm，触发了液位过低报警，调整进料回路中的第一流 量控制阀V5开度至最大；若进料流量已至最大，则降低循环加热器5的工作温度至设定工作温度值140～150℃，从而降低蒸馏速度。
负压闪蒸罐3上部的压力变送器设置了压力过高报警、压力过低报警以及压力极限过高报警，当负压闪蒸罐3内压力不在正常范围内，导致触发了相应报警时，按照如下方式进行处理：
当负压闪蒸罐3工作温度上限值内压力低于0.008MPa，导致触发了压力过低报警时，则增大循环加热器5的工作温度至工作温度上限值160℃；
当负压闪蒸罐3内压力高于0.05MPa，导致触发了压力过高报警时，则减小循环加热器5的工作温度至设定工作温度值140℃，调节第一流量控制阀V5的开度调至最小；
当负压闪蒸罐3内压力高于0.2MPa，触发压力极限过高报警时，关闭第一电动阀V4从而切断进料，关闭循环加热器5，等待操作人员介入处理。
实现了负压闪蒸罐3内压力的动态平衡，降低了循环加热器5的能耗。
负压闪蒸罐3内的温度变送器设置了温度过低报警、温度过高报警、温度极限过高报警，当负压闪蒸罐3中的温度不在正常范围内，导致触发了相应报警时，按照如下的方式进行处理：
当负压闪蒸罐3内的温度低于120℃，触发了温度过低报警时，将循环加热器5调整在加热值为设定工作温度上限值160℃的情形下工作，以使得闪蒸罐内的溶液尽快升温到设定正常范围140～150℃；若循环加热器5已在加热值为设定工作温度上限值160℃的情形下工作，则减小进料回路上第一流量控制阀V5的开度使进料流量降低至15m 3/h；对负压闪蒸罐3内的温度实时监控，并在温度下降时及时进行温度补充，保证了闪蒸的充分进行，提高闪蒸分离的效率，提高了系统中回收的MEG贫液的产品质量。
当负压闪蒸罐3内的温度高于150℃，触发了温度过高报警时，则降低循环加热器5的工作温度至设定工作温度值140℃；防止温度过高，有效减小系统的热负荷，在保证系乙二醇回收率的前提下降低了能耗。
当负压闪蒸罐3内的温度高于170℃，触发了温度极限过高报警时，立即关闭循环加热器5，等待操作人员介入处理。有效防止乙二醇因为温度超过热分解温度而热分解，提高了系统中乙二醇贫液的回收率。
当MEG贫液接收罐7内的密度指示器进行实时测量的MEG贫液的密度小于设定下限值时1.03×10 3kg/m 3，检查循环加热器5是否启动且其加热值为设定工作温度上限值160℃，若未启动或加热值未达设定工作温度上限值160℃，则使循环加热器5升温至按设定工作温 度上限值160℃进行工作，以加快负压闪蒸罐3内含盐乙二醇贫液的蒸馏速度；若此时循环加热器5已经启动，且此时循环加热器5的加热量达到设定工作温度上限值160℃，则减小进料回路中第一流量控制阀V5的开度开到最小，或将进料回路上的第一流量控制阀V5关闭，待乙二醇纯度达到预设值1.1×10 3kg/m 3，再重新打开第一电动阀V4，将第一流量控制阀V5的开度开到正常值，降低循环加热器5的加热温度至设定工作温度值140～150℃；
当MEG贫液接收罐7内的MEG贫液的密度指示器进行实时测量的密度小于合格值时1.1×10 3kg/m 3，检查循环加热器5是否启动且其加热值为设定工作温度上限值160℃，若未启动或加热值未达设定工作温度上限值160℃，则使循环加热器5按加热值为设定工作温度上限值160℃进行工作，以加快负压闪蒸罐3内含盐乙二醇贫液的蒸馏速度；若此时循环加热器5已经启动，且此时循环加热器5的加热量达到设定工作温度上限值160℃，则减小进料回路中第一流量控制阀V5的开度以降低进料速度降，提高负压闪蒸罐3的分离效率；
上述的实施例仅例示性说明本发明创造的原理及其功效，以及部分运用的实施例，而非用于限制本发明；应当指出，对于本领域的普通技术人员来说，在不脱离本发明创造构思的前提下，还可以做出若干变形和改进，这些都属于本发明的保护范围。

Claims (11)

  1. 一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：包括MEG贫液回收装置、含盐乙二醇贫液闪蒸装置以及一阶盐回收装置；
    其中，含盐乙二醇贫液闪蒸装置包含含盐乙二醇贫液罐，其通过管道与第一运输泵连接，在含盐乙二醇贫液罐与第一运输泵之间的管道上安装有第一截止阀，第一运输泵通过管道与负压闪蒸罐相连接，在第一运输泵至负压闪蒸罐之间的管道上依次安设有第一单向阀、第一电动阀和第一流量控制阀，在第一运输泵和单向阀之间的管道上安设有第一温度变送器，在电动阀和流量控制阀之间的管道上安设有第一流量变送器和第一流量控制仪，负压闪蒸罐设有两个液相出口和一个位于罐顶的气相出口，气相出口通过管道连通负压冷凝器，其中一个液相出口通过降液管连接盐液罐，另一个液相出口通过第二运输泵连接循环加热器并且循环加热器的出口连接负压闪蒸罐形成闭环回路；
    在负压闪蒸罐上安设有实时监控并控制负压闪蒸罐内的压力的第一压力控制器、第二压力变送器和第一压力表，负压闪蒸罐上还安设有温度表和温度校验仪，在负压闪蒸罐和第二运输泵之间的管路上安设有第四压力变送器和第五单向阀，在第二运输泵和循环加热器之间的管路上安设有第六单向阀和第七单向阀，在第六单向阀和第七单向阀之间的管路上布置有第五压力变送器和第三温度表；循环加热器的出口通过设置第八单向阀的管道和负压闪蒸罐连接，在第八单向阀和负压闪蒸罐之间的管道上安设有用以确保经加热后的MEG贫液温度与达到指定值的第二压力控制器、第四温度表、第四温度变送器和第五温度表；
    含盐乙二醇贫液闪蒸装置包括通过设置第二单向阀的管道和负压闪蒸罐连通的负压冷凝器，负压闪蒸罐与负压冷凝器两者之间的管道上安设有第一压差变送器、第二压力表和第二温度变送器；负压冷凝器通过设有第三单向阀和第二电动阀的管道连接MEG贫液接收罐，管道上在负压冷凝器和第三单向阀之间安设有第三压力表，在第二电动阀和MEG贫液接收罐之间的管道上布置有用以确认闪蒸后获得的MEG贫液之中的高溶解度一价盐离子含量的第一电导率测定仪、以及第三温度变送器和温度控制器；MEG贫液接收罐上设有第三压力变送器、第二温度表和液位仪；MEG贫液接收罐顶部设有一气相出口通过设有真空阀的管道连接真空泵，MEG贫液接收罐底部的液相出口通过第三截止阀连接第三运输泵，在第三截止阀的入口和第三运输泵的出口之间连接有第二旁通阀，第三运输泵通过第四单向阀与合格MEG贫液存储罐连通；
    一价盐回收系统包含有水罐，水罐通过设置第四运输泵的管道与盐液罐连通，在第四 运输泵的出口至盐液罐之间的管道上依次安设有第十单向阀、第四电动阀和第二流量控制阀；在第四运输泵和单向阀之间的管道上设有第四压表，在电动阀和流量控制阀之间的管道上安设有根据盐液罐中盐溶液浓度控制进水量大小的第二流量变送器和第二流量控制仪；负压闪蒸罐至盐液罐之间通过依次设有第九单向阀和第三电动阀的管道相连接，盐液罐上布置有用以实时监控盐液罐内的盐溶液浓度并维持盐液罐内液面稳定的第七温度表、第二液位变送器、第二液位控制器、第五压力表和第二电导率测定仪；
    盐液罐通过两条并列布置的设置第五截止阀的管道和第五旁通阀的管道分别与第五运输泵相连，第五运输泵和离心机之间的管道上连接有第十一单向阀和第五电动阀，运输泵和单向阀之间的管道上设有第六压力变送器，第五电动阀和离心机之间的管道上设有第三流量变送器和第三流量控制器；离心机上设有位于顶部的气相出口、位于底部的固相出口，其中位于顶部的气相出口通过设置第十三单向阀的管道与外界连通，位于底部的固相出口通过设置第十四单向阀的管道与盐罐连通。
  2. 如权利要求1所述的一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：在第一运输泵的输出口还通过设置第一旁通阀的管道连接至含盐乙二醇贫液罐和第一截止阀之间的管道上形成第一旁通回路，在第一旁通回路的回路连接口与第一截止阀之间的管道上安装有第一压力变送器。
  3. 如权利要求1所述的一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：所述负压闪蒸罐的罐体内侧下部设有控制最低液位以保证罐内闪蒸的MEG贫液量的稳定的第一液位变送器和第一液位控制器。
  4. 如权利要求1所述的一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：所述第六单向阀出口端的管道和第七单向阀出口端的管道间连接有第二压差变送器。
  5. 如权利要求1所述的一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：所述第四运输泵通过设置第四截止阀和第四旁通阀的管道构成旁通回路。
  6. 如权利要求1所述的一种深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统，其特征在于：所述离心机上设有位于底部循环回路出口，循环回路出口通过设置第十二单向阀和第六电动阀的管道与盐液罐连接。
  7. 如权利要求1-6中任一项所述的深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，具体过程如下：
    步骤1，含盐乙二醇贫液闪蒸：
    步骤1-1，原料运输：初始状态时，各个系统中的阀门均处于关闭状态；首先打开第一截止阀和第一旁通阀，启动第一运输泵，当含盐乙二醇贫液罐和第一运输泵之间的旁通回路充满MEG贫液后，第一压力变送器检测到管内压力稳定，然后通过远程控制打开电动阀，并且打开第一流量控制阀，同时关闭第一旁通阀，将含盐乙二醇贫液原料运送至负压闪蒸罐内；
    步骤1-2，流量控制：当负压闪蒸罐上的第一液位变送器检测到罐内溶液达到指定液位后，通过控制系统控制进料管上的第一流量控制阀，调整罐内流量大小，维持负压闪蒸罐的液位平稳；若突遇紧急状况，则直接远程关闭第一电动阀，阻止原料的流入；
    步骤1-3，循环加热：流入负压闪蒸罐内的含盐乙二醇贫液，通过第二运输泵转送至循环加热器中加热并重新流回至负压闪蒸罐内，位于负压闪蒸罐上的温度校验仪和第四温度变送器实时监控罐内温度，确保罐内温度稳定在140±5℃；
    步骤1-4，闪蒸：负压闪蒸罐上的第一压力控制器和第二压力变送器确保负压闪蒸罐的操作压力保持在15±5KPa；由于压力的下降，负压闪蒸罐内的乙二醇开始进行闪蒸分离，通过循环加热回路进行温度补充，来维持闪蒸过程中所需的温度，MEG贫液被蒸馏出来并以气相形式堆积在负压闪蒸罐的顶部；
    步骤2，MEG贫液回收：
    步骤2-1，MEG贫液冷凝：经由闪蒸产生的MEG贫液气体经过第二单向阀进入负压冷凝器中，使热蒸汽迅速降温至40±3℃使得MEG贫液气体重新液化，然后打开第二电动阀，将冷凝液汇入MEG贫液接收罐；
    步骤2-2，提纯：打开真空阀、气动真空泵，将MEG贫液接收罐中的少量气体排出，剩余的MEG贫液则通过第三运输泵存储到合格MEG贫液存储罐中；
    步骤3，一价盐回收：
    步骤3-1，盐液存储：由步骤1-4中得到的位于负压闪蒸罐底部的盐溶液通过降液管被运送至盐液罐中，盐液罐中的一价盐已经达到饱和状态，开始结晶析出，待第二电导率测定仪测得盐液罐中盐浓度达到设定值后，通过第五运输泵运送至离心机中离心；
    步骤3-2，离心分离：送往离心机中的盐液内混杂一些不溶气体通过离心机上方的第十三单向阀排出，剩余固液混合物经离心后，固体盐块被存入盐罐中进行保存作为后续深加工原料，剩余未完全离心的溶液则通过离心机的液相出口重新回流入盐液罐中；
    步骤3-3，注水：当第二液位变送器检测盐液罐中的液面下降至下限值时，第二液位控制器则发出信号，控制系统开启第四电动阀，从水罐中抽取水注入盐液罐中，保证盐液罐 中液面的稳定；当第二电导率测定仪测得盐液罐中盐浓度低于设定值后，停止离心机的工作，并关闭第五电动阀和第五运输泵，直至下一个离心处理条件满足，转至步骤3-1进行循环。
  8. 如权利要求7所述的深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，其特征在于：所述负压闪蒸罐内的液位通过液位变送器设置了液位极限过高报警、液位过高报警、液位过低报警以及液位极限过低报警，当液位不在正常范围内，导致触发了以上报警时，按照如下方式进行处理：
    当负压闪蒸罐内含盐乙二醇贫液液位过高触发了液位极限过高报警，则切断进料回路中的第一电动阀以防止含盐乙二醇贫液浸没除雾器或进入到冷凝器中；此后，随着蒸馏过程的继续，负压闪蒸罐内的液位降低至触发液位过低报警时，再重新打开进料回路；
    当负压闪蒸罐内液面高度过低触发了液位极限过低报警，则紧急关闭循环加热器以将负压闪蒸罐内含盐乙二醇贫液的温度控制在170℃以下；此后，新注入到负压闪蒸罐内的含盐乙二醇贫液由于加热不足导致其蒸馏进程缓慢，负压闪蒸罐内的液位将逐步升高，当液位过高导致触发液位过高报警时，再重新启动循环加热器；
    当负压闪蒸罐内液面过高触发了液位过高报警，检查循环加热器是否启动且其加热值为工作温度上限值，若未启动或加热值未达工作温度上限值，则使循环加热器按加热值为工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到工作温度上限值，则减小进料回路中第一流量控制阀的开度以将降低进料速度；
    过负压闪蒸罐内液位过低触发了液位过低报警，调整进料回路中的第一流量控制阀开度至最大；若进料流量已至最大，则降低循环加热器的工作温度至设定工作温度值，从而降低蒸馏速度。
  9. 如权利要求8所述的深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，其特征在于：所述负压闪蒸罐上部的压力变送器设置了压力过高报警、压力过低报警以及压力极限过高报警，当负压闪蒸罐内压力不在正常范围内，导致触发了相应报警时，按照如下方式进行处理：
    当负压闪蒸罐工作温度上限值内压力过低导致触发了压力过低报警时，则增大循环加热器的工作温度至工作温度上限值；
    当负压闪蒸罐内压力过高导致触发了压力过高报警时，则减小循环加热器的工作温度至设定工作温度值，调节第一流量控制阀的开度调至最小；
    当负压闪蒸罐内压力超高触发了压力极限过高报警时，关闭第一电动阀从而切断进料，关闭循环加热器，等待操作人员介入处理。
  10. 如权利要求9所述的深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，其特征在于：所述负压闪蒸罐内的温度变送器设置了温度过低报警、温度过高报警、温度极限过高报警，当负压闪蒸罐中的温度不在正常范围内，导致触发了相应报警时，按照如下的方式进行处理：
    当负压闪蒸罐内的温度低于120℃，触发了温度过低报警时，将循环加热器调整在加热值为设定工作温度上限值的情形下工作，以使得负压闪蒸罐内的溶液尽快升温到设定正常范围；若循环加热器已在加热值为设定工作温度上限值的情形下工作，则减小进料回路上第一流量控制阀的开度使进料流量降低；
    当负压闪蒸罐内的温度过高触发了温度过高报警时，则降低循环加热器的工作温度至设定工作温度值；
    当负压闪蒸罐内的温度超高触发了温度极限过高报警时，立即关闭循环加热器，等待操作人员介入处理。
  11. 如权利要求7所述的深海天然气开采中含高溶解度盐的乙二醇贫液的脱盐系统的脱盐方法，其特征在于：
    当MEG贫液接收罐内的密度指示器进行实时测量的MEG贫液的密度小于设定下限值时，检查循环加热器是否启动且其加热值为设定工作温度上限值，若未启动或加热值未达设定工作温度上限值，则使循环加热器升温至按设定工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到设定工作温度上限值，则减小进料回路中第一流量控制阀的开度开到最小，或将进料回路上的第一流量控制阀关闭，待乙二醇纯度达到预设值，再重新打开第一电动阀，将第一流量控制阀的开度开到正常值，降低循环加热器的加热温度至设定工作温度值；
    当MEG贫液接收罐内的MEG贫液的密度指示器进行实时测量的密度小于合格值时，检查循环加热器是否启动且其加热值为设定工作温度上限值，若未启动或加热值未达设定工作温度上限值，则使循环加热器按加热值为设定工作温度上限值进行工作，以加快负压闪蒸罐内含盐乙二醇贫液的蒸馏速度；若此时循环加热器已经启动，且此时循环加热器的加热量达到设定工作温度上限值，则减小进料回路中第一流量控制阀的开度以降低进料速度降，提高负压闪蒸罐的分离效率。
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