CN106693617A - Triethylene glycol dehydration device and process for oxygen-enriched gas flue gas - Google Patents

Triethylene glycol dehydration device and process for oxygen-enriched gas flue gas Download PDF

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Publication number
CN106693617A
CN106693617A CN201611058845.1A CN201611058845A CN106693617A CN 106693617 A CN106693617 A CN 106693617A CN 201611058845 A CN201611058845 A CN 201611058845A CN 106693617 A CN106693617 A CN 106693617A
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absorption tower
gas
tower
triethylene glycol
poor
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张引弟
李莎
沈秋婉
田磊
伍丽娟
刘捷
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Yangtze University
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Yangtze University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/263—Drying gases or vapours by absorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/22—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention discloses a triethylene glycol dehydration device and process for oxygen-enriched gas flue gas. The process comprises the following steps: firstly enabling lean triethylene glycol to enter from a tower top of an absorption tower; carrying out counter-current contact on the lean triethylene glycol and oxygen-enriched gas flue gas entering from a tower bottom of the absorption tower under the conditions of high pressure and normal temperature of the absorption tower; absorbing moisture in the gas flue gas and enabling the gas flue gas to pass through a lean and rich solution heat exchanger in a form of rich glycol; carrying out heat exchange with lean glycol and enabling the gas flue gas to enter a regeneration tower; and enabling the gas flue gas to pass through a glycol pump, a dry gas-lean liquid heat exchanger and a condenser in sequence in a lean glycol form after the gas flue gas is dehydrated in the regeneration tower; and obtaining dry gas leaving from the tower top of the absorption tower, so as to obtain high-purity CO2. By adopting the dehydration device and process disclosed by the invention, the problems of high thermal exploitation cost of thickened oil and great energy consumption of a steam-injection boiler are solved, and a greenhouse effect problem caused by the fact that a lot of the CO2 is emitted is solved; economic benefits, energy source benefits and environment benefits can be generated; and the dehydration device and process have important meanings on construction of energy-saving and environment-friendly type development modes and green production of an oil field.

Description

Oxygen rich fuel gas flue gas TEG dehydration device and its technique
Technical field
The present invention relates to the dehydration of oxygen rich fuel gas flue gas triethylene glycol, it is dehydrated in particular to a kind of oxygen rich fuel gas flue gas triethylene glycol and is filled Put and its technique.
Background technology
In the last few years, because production and traffic need the substantial amounts of fossil fuel that burns, and combustion of fossil fuel CO2Excessive row Putting causes Global Environmental Problems to become increasingly conspicuous, and reduces CO2Discharge is own through turning into the common focus of attention in the whole world.Due to fossil energy Will be the main energy sources of coming few decades, so in oil gas field, can suit measures to local conditions, by CO2Capture, seal up for safekeeping and resource It is to solve the current carbon emission reduction most direct approach of task of country that (CCUS) technology of utilization is introduced, and can also be noted by oil-gas reservoir Enter CO2The rate of oil and gas recovery is favorably improved, is the ideal place of CCUS technology applications.
Also contain a certain amount of saturation water in the flue gas produced after combustion gas oxygen-enriched combusting, in order to realize CO2Resource profit With can be dehydrated to combustion gas flue gas, purified treatment obtains the CO of high concentration2For oil-gas field development.In CO2Manage defeated process In have strict requirements to water content, primarily to preventing appearance and the CO of two phase flow2It is dissolved in after water to pipeline, equipment Corrosion, therefore in CO2Need to carry out deep dehydration treatment to combustion gas flue gas before pipe is defeated.
In general, it is less susceptible to CO only by methods such as compression and conventional warm-downs2In moisture removal it is defeated to managing Standard, therefore need to be the same with conventional gas dewatering using other depth dewatering higher, oxygen rich fuel gas flue gas it is de- Water method has glycol absorption process, cooling method and sieve method, and triethylene glycol absorption process is the prefered method for meeting the defeated requirement of pipe.My god The key component of right gas is CH4, also contain a small amount of H2O, ethane, butane etc., the key component of oxygen rich fuel gas flue gas is CO2、H2O, Also contain a small amount of other components.Because gas dehydration and oxygen rich fuel gas fume-dehydrating belong to gas dewatering, simultaneously for day Right qi exhaustion water and oxygen rich fuel gas fume-dehydrating, triethylene glycol dewatering are prefered method.Therefore, both meetings on dewatering process In the presence of many similarities；Further, since there is significant difference in component and in nature with oxygen rich fuel gas flue gas in natural gas, because This, can also there are some difference in both on dewatering process.At present, conventional natural gas TEG Dehydration Processing flow is technically It is very ripe, but oxygen-enriched combusting combustion gas flue gas TEG Dehydration Processing haves the shortcomings that technological parameter imperfection, deficiency in economic performance.
The content of the invention
It is an object of the present invention to provide a kind of oxygen rich fuel gas flue gas TEG dehydration device and its technique.The method utilizes tower Plate method for designing scheduling theory, according to oxygen rich fuel gas flue gas composition, treating capacity Q and meets displacement of reservoir oil CO2The known variables such as technical requirements Some parameters needed in simulation process are extrapolated, for example：Absorption tower tower diameter, tower height, column plate liquid stream, downspout, tower plate structure Etc. parameter.Meanwhile, required by technological process standard and sensitivity analysis determines to be difficult the parameter of acquisition, for example：Stripping gas N2 Molar flow, then by setting up oxygen rich fuel gas flue gas TEG Dehydration Processing procedural model, triethylene glycol is carried out to combustion gas flue gas Dehydration, purified treatment.The technique obtains meeting the high-purity CO for managing defeated requirement2, reach CO2Near-zero release, improve oil gas harvesting Rate, realizes multi-production process flow.
To achieve the above object, a kind of oxygen rich fuel gas flue gas TEG dehydration device that the present invention is provided, described device bag Absorption tower is included, top is provided with the absorption tower side wall and is provided with poor triethylene glycol inlet tube, under the poor triethylene glycol inlet tube Side is provided with oxygen rich fuel gas smoke air inlet, and the absorption tower bottom is connected with check-valves, poor rich solution in turn and exchanges heat by pipeline Device, heater and regenerator；
The absorption tower top is connected with dry gas-lean solution heat exchanger, the second condenser in turn by pipeline, and described second is cold Condenser top connects with liquefying plant side wall；The liquefying plant top connects with separator side wall；The poor rich solution heat exchange Device upper wall one end is connected with glycol pump, and the glycol pump is connected with dry gas-lean solution heat exchanger lower wall other end, the dry gas-poor Liquid heat exchanger upper wall one end is connected with the first condenser.
Further, absorption tower reboiler is installed between the absorption tower and check-valves, the absorption tower reboiler with The lower section connection of absorption tower opposite side wall.
Yet further, absorption tower condenser, the absorption are installed between the absorption tower and dry gas-lean solution heat exchanger Tower condenser is connected with the upper side wall of the opposite side of absorption tower 1.
Yet further, wall top in the regenerator side is provided with stripping gas N2It is inlet tube, the stripping gas N2Import Pipe lower section is the pipeline between heater and regenerator；The regenerator bottom is connected with regenerator reboiler, and regenerator is again Boiling device is connected with the poor rich liquid heat exchanger lower wall other end again, and the regenerator reboiler is connected with regenerator opposite side wall lower section, The regenerator upper end is connected with regenerator condenser, and the regenerator condenser is connected with regenerator opposite side wall top.
Yet further, the density of the absorption tower tower diameter size and glycol solution, oxygen rich fuel gas smoke density and oxygen-enriched The volume flow of combustion gas flue gas is related, optimizes absorption tower tower diameter size, meets equation below：
V=0.0508 [(ρl-ρg)/ρg]0.5 (1-1)
ρ in formulalIt is the density of glycol solution, unit is kg/m3；ρgIt is oxygen rich fuel gas smoke density, unit is kg/m3；D It is absorption tower tower diameter, unit is m；Q is the volume flow of oxygen rich fuel gas flue gas, and unit is m3/s；A is absorbing tower plate suqare.
Yet further, the absorption tower is plate column, can be with the height on absorption tower by body height H1, headroom it is high Degree H2With bottom space height H3Three parts constitute, wherein,
Body height H1It is from tower top ground floor column plate to the vertical range between last layer of column plate of bottom of towe, according to formula (1-4) is calculated：
H1=(N-2-S) × HT+S×H'T+Hf (1-4)
H in formulaTIt is column plate spacing, unit is m；H'TTo be provided with the column plate spacing of manhole, unit is m；S is people's number of perforations, The manhole in tower top space and bottom of towe space is not included；HfIt is the spatial altitude of feed zone, unit is m；N is the number of plates；
Headroom height H2Calculating formula such as formula (1-5) shown in：
H2=0.35 × D+1.5 × HT+HC (1-5)
D is tower diameter in formula, and unit is m；HCFor demister highly, unit is m, general value 0.1 or 0.15m.
Bottom space height H3Calculated according to glycol internal circulating load and tower diameter, as shown in formula (1-6),
In formula, M is poor triethylene glycol internal circulating load, and unit is m3/ s, π are pi, and D is absorption tower tower diameter, and unit is m.
Yet further, the column plate stream forms selection on the absorption tower：
As absorption tower tower diameter D≤2.2m, the column plate stream forms use single overflow type；And downflow weir in absorption tower 1 Length L=(0.6~0.8) D,
Or, as absorption tower tower diameter D>During 2.2m, the column plate stream forms typically use double overflow type, and are overflow in absorption tower Stream weir length L=(0.5~0.7) D；
Height of weir plate is tower clear liquid height on plate H in absorption toweraSubtract weir supernatant layer height Hb, i.e. H=Ha-Hb。
Tower clear liquid height on plate HaIt is general to take 50~100mm, and weir supernatant layer height HbType with weir has become It is dynamic.For flat weir, to ensure that liquid stream is uniform, H is should ensure thatb=13mm
Yet further, the following downspout of downspout parameter on the absorption tower 1
Table downspout parameter
Bottom gap (mm) Top width (mm) Bottom width (mm) Straight section height (mm)
30~50 220~260 200~240 180~220
Valve plate structure design
(1) valve opening gas velocity
Valve opening gas velocity on column plate during all float valve standard-sized sheets is referred to as valve hole critical gas-velocity, valve hole critical gas-velocity UcrCalculating formula is such as Shown in formula (1-7).
H in formulabFor flat weir supernatant layer highly, unit is m；H is height of weir plate, and unit is m；△ ρ are air-liquid two-phase Density contrast, unit is kg/m3。
Float valve number
V in formula1It is absorption tower gas load, unit is m3/s；U0It is operation valve opening gas velocity, can use U0=1.1Ucr；d0For Valve opening diameter, takes 0.04m.
Yet further, the regenerator reboiler temperature is 188~200 DEG C.
The invention provides a kind of technique of oxygen rich fuel gas flue gas TEG dehydration device, comprise the following steps：
1) poor triethylene glycol enters absorption tower by poor triethylene glycol inlet tube through absorption tower top, meanwhile, oxygen rich fuel gas flue gas Absorption tower is entered through absorption tower bottom by oxygen rich fuel gas smoke air inlet；Under high pressure normal temperature condition, poor triethylene glycol with adverse current Oxygen rich fuel gas flue gas contacted, obtain containing CO2Dry gas and rich triethylene glycol；
2) rich triethylene glycol is heated after absorbing tower bottom exits into check-valves by poor rich liquid heat exchanger, obtains temperature Elevated rich triethylene glycol, then rich triethylene glycol is heated in 140~160 DEG C of entrance regenerators by heater, in high-temperature low-pressure Under the conditions of, by stripping gas N2The N that inlet tube enters2Rich triethylene glycol is stripped, poor triethylene glycol and vapor is obtained, water steams Gas entered the discharge of regenerator condenser, and water steam enters in regenerator after partial liquefaction；
3) poor triethylene glycol is by regenerator reboiler, regenerated and poor triethylene glycol of the concentration higher than 99%, vaporization it is poor Triethylene glycol and vapor；The poor triethylene glycol and water steam of vaporization enter in regenerator；
4) the poor triethylene glycol of regeneration and concentration higher than 99% is back to poor rich liquid heat exchanger, and the regeneration for being cooled down poor three is sweet Alcohol；
5) step 1) in during the dry gas that obtains exits into dry gas-lean solution heat exchanger through absorption tower tower top, while cooling Regenerate poor triethylene glycol pressurization to enter in dry gas-lean solution heat exchanger, dry gas carries out heat exchange with the poor triethylene glycol of regeneration of cooling, so The poor triethylene glycol that temperature is 35~45 DEG C is obtained by the cooling of the first condenser, and recycle and reuse is discharged with pipeline, heat is handed over The dry gas for changing enters liquefying plant after being cooled down through the second condenser, obtains by CO2、N2And O2The gaseous mixture and water of composition, water is by liquid Change the discharge of bottom of device pipeline；
6) gaseous mixture enters separator by liquefying plant top, obtains N2And O2From separation unit overhead discharge, concentration is big In 95% CO2From the outflow of the bottom of separator 11.
Further, the step 1) in, the mass fraction of poor triethylene glycol is that 99.8%, temperature is 37 DEG C, volume flow It is 33m3/h。
Yet further, the step 1) in, oxygen rich fuel gas flue-gas temperature is 37 DEG C.
Yet further, the step 2) in, N2Temperature for 60 DEG C, pressure be 1.5bar, molar flow be 50kmol/ h。
The beneficial effects of the present invention are
The present invention is dexterously by oxygen-enriched combustion technology and CO2- EOR technologies are combined, and realize the recovery to flue gas, are processed, Recycling, has responded low-carbon emission reduction, the call of energy-conserving and environment-protective in country's " 13 planning "；Combined by theory and put into practice mould Intend, there is provided the oxygen rich fuel gas flue gas TEG dehydration device and its method for designing and technique of complete set, for relevant parameter Optimization and practice process have great importance；Not only solve the big problem of heavy crude heat extraction high cost, energy consumption, also solve by In CO2The greenhouse effects problem that causes of a large amount of discharges, to build energy saving and environment friendly development mode and green society have it is important Value.Device of the invention obtains meeting the high-purity CO for managing defeated requirement2, reach CO2Near-zero release, improve oil gas harvesting Rate, realizes multi-production process flow.
Brief description of the drawings
Fig. 1 is the schematic diagram of oxygen rich fuel gas flue gas TEG dehydration device of the present invention；
In figure, absorption tower 1, poor triethylene glycol inlet tube 1.3, oxygen rich fuel gas smoke air inlet 1.4, check-valves 2, poor rich solution are changed Hot device 3, heater 4, regenerator 5, regenerator reboiler 5.1, regenerator condenser 5.2, stripping gas N2Inlet tube 5.3, glycol Pump 6, dry gas-lean solution heat exchanger 7, the first condenser 8, the second condenser 9, liquefying plant 10, separator 11.
Specific embodiment
In order to preferably explain the present invention, below in conjunction with the specific embodiment main contents that the present invention is furture elucidated, but Present disclosure is not limited solely to following examples.
As shown in Figure 1：A kind of oxygen rich fuel gas flue gas TEG dehydration device, device includes absorption tower 1, the side wall of absorption tower 1 On be provided with top and be provided with poor triethylene glycol inlet tube 1.3, the lower section of poor triethylene glycol inlet tube 1.3 is provided with oxygen rich fuel gas flue gas and enters Gas port 1.4, the bottom of absorption tower 1 is connected with check-valves 2, poor rich liquid heat exchanger 3, heater 4 and regenerator 5 in turn by pipeline；
The top of absorption tower 1 is connected with dry gas-lean solution heat exchanger 7, the second condenser 9, the second condenser 9 in turn by pipeline Top connects with the side wall of liquefying plant 10；The top of liquefying plant 10 connects with the side wall of separator 11；The upper wall of poor rich liquid heat exchanger 3 One end is connected with glycol pump 6, and glycol pump 6 is connected with the lower wall other end of dry gas-lean solution heat exchanger 7, on dry gas-lean solution heat exchanger 7 Wall one end is connected with the first condenser 8.
Absorption tower reboiler 1.1 is installed, absorption tower reboiler 1.1 is another with absorption tower 1 between absorption tower 1 and check-valves 2 The lower section connection of side wall.Absorption tower condenser 1.2, absorption tower are installed between reabsorber 1 and dry gas-lean solution heat exchanger 7 Condenser 1.2 is connected with the upper side wall of the opposite side of absorption tower 1.
The side wall top of regenerator 5 is provided with stripping gas N2It is inlet tube 5.3, stripping gas N2The lower section of inlet tube 5.3 is heating Pipeline between device 4 and regenerator 5；The bottom of regenerator 5 is connected with regenerator reboiler 5.1, and regenerator reboiler 5.1 again with The lower wall other end of poor rich liquid heat exchanger 3 is connected, and regenerator reboiler 5.1 is connected with the opposite side wall of regenerator 5 lower section, regenerator 5 Upper end is connected with regenerator condenser 5.2, and regenerator condenser 5.2 is connected with the opposite side wall of regenerator 5 top.
The volume of the density, oxygen rich fuel gas smoke density and oxygen rich fuel gas flue gas of the tower diameter size of absorption tower 1 and glycol solution Flow is related, optimizes the tower diameter size of absorption tower 1, meets equation below：
V=0.0508 [(ρl-ρg)/ρg]0.5 (1-1)
ρ in formulalIt is the density of glycol solution, unit is kg/m3；ρgIt is oxygen rich fuel gas smoke density, unit is kg/m3；D It is absorption tower tower diameter, unit is m；Q is the volume flow of oxygen rich fuel gas flue gas, and unit is m3/s；A is absorbing tower plate suqare.
Absorption tower 1 is plate column, and the height on absorption tower 1 is by body height H1, headroom height H2With bottom space highly H3Three parts constitute, wherein,
Body height H1It is from tower top ground floor column plate to the vertical range between last layer of column plate of bottom of towe, according to formula (1-4) is calculated：
H1=(N-2-S) × HT+S×H'T+Hf (1-4)
H in formulaTIt is column plate spacing, unit is m；H'TTo be provided with the column plate spacing of manhole, unit is m；S is people's number of perforations, The manhole in tower top space and bottom of towe space is not included；HfIt is the spatial altitude of feed zone, unit is m；N is the number of plates；
Headroom height H2Calculating formula such as formula (1-5) shown in：
H2=0.35 × D+1.5 × HT+HC (1-5)
D is tower diameter in formula, and unit is m；HCFor demister highly, unit is m, general value 0.1 or 0.15m.
Bottom space height H3Calculated according to glycol internal circulating load and tower diameter, as shown in formula (1-6),
In formula, M is poor triethylene glycol internal circulating load, and unit is m3/ s, π are pi, and D is absorption tower tower diameter, and unit is m.
The column plate stream forms selection on absorption tower 1：
As absorption tower tower diameter D≤2.2m, the column plate stream forms use single overflow type；And downflow weir in absorption tower 1 Length L=(0.6~0.8) D,
As absorption tower tower diameter D>During 2.2m, the column plate stream forms are typically using overflow in double overflow type and absorption tower 1 Weir length L=(0.5~0.7) D
Height of weir plate is tower clear liquid height on plate H in absorption tower 1aSubtract weir supernatant layer height Hb, i.e. H=Ha-Hb。
Tower clear liquid height on plate HaValue is 50~100mm, and weir supernatant layer height HbType with weir has become It is dynamic.For flat weir, to ensure that liquid stream is uniform, H is should ensure thatbYet further, downspout is=13mm in the absorption tower 1
The downspout parameter of table 1
Bottom gap (mm) Top width (mm) Bottom width (mm) Straight section height (mm)
30~50 220~260 200~240 180~220
Valve plate structure design
(1) valve opening gas velocity
Valve opening gas velocity on column plate during all float valve standard-sized sheets is referred to as valve hole critical gas-velocity, valve hole critical gas-velocity UcrCalculating formula is such as Shown in formula (1-7).
H in formulabFor flat weir supernatant layer highly, unit is m；H is height of weir plate, and unit is m；△ ρ are air-liquid two-phase Density contrast, unit is kg/m3。
Float valve number
V in formula1It is absorption tower gas load, unit is m3/s；U0It is operation valve opening gas velocity, can use U0=1.1Ucr；d0For Valve opening diameter, takes 0.04m.
According to above-mentioned formula, above-mentioned oxygen rich fuel gas flue gas TEG dehydration device, with reference to the oxygen rich fuel gas flue gas of certain factory Component and content, so as to obtain the concrete structure parameter of factory's oxygen rich fuel gas flue gas TEG dehydration device：
By checking, the oxygen rich fuel gas flue gas composition of the factory is：11.74%CO2, 21.38%H2O, 64.69%N2、 2.19%O2(normal volume fraction), oxygen rich fuel gas treatment quantity Q=800m3/ h=0.222m3/s。ρl=850.882kg/ m3, ρg=70.145kg/m3, Q=800m3/ h=0.222m3/ s, learns so as to be calculated according to above-mentioned formula：
1) tower diameter is calculated
Oxygen rich fuel gas flue gas mean flow rate v=0.169m/s is calculated according to formula (1-1), suction is calculated according to formula (1-2) Receive tower column plate area A=1.314m2, absorption tower tower diameter D=1.294m=1294mm is calculated according to formula (1-3), tentatively calculate After tower diameter D, rounding is carried out to the value, conventional standard tower diameter is：400、500、600、700、800、1000、1200、1400、 1600th, 2000,2200mm, therefore absorption tower tower diameter D is 1200mm.
2) tower body height H1
Column plate spacing H'TSelection chosen by empirical value according to the size of tower diameter, as shown in table 1-1.
The relation of the column plate spacing of table 2 and tower diameter
Tower diameter D (m) <0.5 0.5~0.8 0.8~1.6 1.6~2.0 2.0~2.4 >2.4
Column plate spacing HT(m) 0.3 0.35 0.45 0.5 0.6 0.8
Take HT=0.45m, sets 1 manhole, i.e. S=1 herein.In addition, N=8, H'T=0.6m, Hf=0.45m.
The body height H of tower is calculated by formula (1-4)1It is 3.3m.
3) headroom is highly
Headroom height H2Headroom height H is calculated by formula (1-5)2=1.265m.
4) bottom space is highly
Bottom space height H3Bottom space height H is calculated by formula (1-6)3Be 0.008m, i.e. 8mm.Therefore, absorption tower Tower height is 4.573m.
5) the downflow weir length of single overflow type column plate
Tower diameter is less than or equal to recommend single overflow type during 2.2m, for single overflow type column plate, downflow weir length L= 0.7D, i.e. downflow weir length L=0.84m.
6) height of weir plate
For flat weir, to ensure that liquid stream is uniform, H is should ensure thatb=13mm, takes tower clear liquid height on plate Ha=80mm, calculates Obtain height of weir plate H=67mm.
7) downspout
The downspout parameter of table 3
Bottom gap (mm) Top width (mm) Bottom width (mm) Straight section height (mm)
40 250 220 200
8) valve opening gas velocity
Valve hole critical gas-velocity Ucr=1.116m/s.
9) float valve number
Float valve number N is calculated by formula (1-8)1=144.
To sum up calculate, be absorbed tower relevant parameter such as following table
The absorption tower relevant parameter of table 4
The volume flow Q of oxygen rich fuel gas flue gas 800m3/h Tower clear liquid height on plate Ha 80mm
Oxygen rich fuel gas flue-gas temperature T 30℃ Weir supernatant layer height Hb 13mm
Absorbing tower presses P 4MPa Height of weir plate H 67mm
Absorption tower tower diameter D 1.2m Downspout bottom gap 40mm
Absorption tower body height H1 3.3m Downspout top width 250mm
Absorption tower headroom height H2 1.265m Downspout bottom width 220mm
Absorption tower bottom space height H3 0.008m Downspout straight section height 200mm
Absorption tower tower height 4.573m Valve plate valve hole critical gas-velocity Ucr 1.116m/s
Downflow weir length L 0.84m Float valve number N1 144
And the regenerator number of plates is 3, tower pressure is 80kpa, and reflux ratio is 5.5 (mol), bottom product flow rate and feed flow rates Than being 0.155；Described reboiler temperature is 197.9 DEG C.
Oxygen rich fuel gas flue gas TEG Dehydration Processing flow is implemented to the factory according to said apparatus：Comprise the following steps：
1) mass fraction is 99.8%, temperature for 37 DEG C, volume flow are 33m3The poor triethylene glycol of/h passes through poor triethylene glycol Inlet tube 1.3 enters absorption tower 1 through the top of absorption tower 1, meanwhile, temperature is that 30 DEG C of oxygen rich fuel gas flue gas passes through oxygen rich fuel gas cigarette Gas air inlet 1.4 enters absorption tower 1 through the bottom of absorption tower 1；Under high pressure normal temperature condition, the oxygen rich fuel gas of poor triethylene glycol and adverse current Flue gas is contacted, and obtains containing CO2Dry gas and rich triethylene glycol；
2) rich triethylene glycol is heated after exiting into check-valves 2 by the bottom of towe of absorption tower 1 by poor rich liquid heat exchanger 3, is obtained The elevated rich triethylene glycol of temperature, then rich triethylene glycol is heated in 148 DEG C of entrance regenerators 5 by heater 4, in high-temperature low-pressure Under the conditions of, by stripping gas N2The temperature that inlet tube 5.3 enters is 60 DEG C, pressure is 1.5bar, molar flow is 50kmol/hN2 Rich triethylene glycol is stripped, poor triethylene glycol and vapor is obtained, vapor entered regenerator condenser 5.2 and discharges, part liquid Water steam enters in regenerator 5 after change；
3) poor triethylene glycol is regenerated and concentration is higher than 99% poor triethylene glycol, vaporized by regenerator reboiler 5.1 Poor triethylene glycol and vapor；The poor triethylene glycol and water steam of vaporization enter in regenerator 5；
4) the poor triethylene glycol of regeneration and concentration higher than 99% is back to poor rich liquid heat exchanger 3, the regeneration for being cooled down poor three Glycol；
5) step 1) in during the dry gas that obtains exits into dry gas-lean solution heat exchanger 7 through the tower top of absorption tower 1, while cooling The pressurization of regeneration poor triethylene glycol enter in dry gas-lean solution heat exchanger 7, dry gas carries out heat friendship with the poor triethylene glycol of regeneration of cooling Change, then obtain the poor triethylene glycol that temperature is 37 DEG C through the cooling of the first condenser 8, and recycle and reuse, heat are discharged with pipeline The dry gas of exchange enters liquefying plant 10 after being cooled down through the second condenser 9, obtains by CO2、N2And O2The gaseous mixture and water of composition, Water is discharged by the bottom pipe of liquefying plant 10；
6) gaseous mixture enters separator 11 by the top of liquefying plant 10, obtains N2And O2From the discharge of the top of separator 11, CO of the concentration more than 95%2From the outflow of the bottom of separator 11.
Other unspecified parts are prior art.Although above-described embodiment is made that to the present invention and retouch in detail State, but it is only a part of embodiment of the invention, rather than whole embodiments, people can also according to the present embodiment without Other embodiment is obtained under the premise of creativeness, these embodiments belong to the scope of the present invention.

Claims (10)

1. a kind of oxygen rich fuel gas flue gas TEG dehydration device, it is characterised in that：Described device includes absorption tower (1), the suction Top is provided with receipts tower (1) side wall and is provided with poor triethylene glycol inlet tube (1.3), poor triethylene glycol inlet tube (1.3) lower section It is provided with oxygen rich fuel gas smoke air inlet (1.4), absorption tower (1) bottom is connected with check-valves (2), poor in turn by pipeline Rich solution heat exchanger (3), heater (4) and regenerator (5)；
Absorption tower (1) top is connected with dry gas-lean solution heat exchanger (7), the second condenser (9) in turn by pipeline, described Second condenser (9) top connects with liquefying plant (10) side wall；Liquefying plant (10) top and separator (11) side Wall is connected；Described poor rich liquid heat exchanger (3) upper wall one end is connected with glycol pump (6), and the glycol pump (6) is changed with dry gas-lean solution Hot device (7) lower wall other end connection, the dry gas-lean solution heat exchanger (7) upper wall one end is connected with the first condenser (8).
2. oxygen rich fuel gas flue gas TEG dehydration device according to claim 1, it is characterised in that：The absorption tower (1) with Absorption tower reboiler (1.1), the absorption tower reboiler (1.1) and absorption tower (1) opposite side wall are installed between check-valves (2) Lower section connection.
3. oxygen rich fuel gas flue gas TEG dehydration device according to claim 2, it is characterised in that：The absorption tower (1) with Absorption tower condenser (1.2), the absorption tower condenser (1.2) and absorption tower are installed between dry gas-lean solution heat exchanger (7) (1) the upper side wall connection of opposite side.
4. the oxygen rich fuel gas flue gas TEG dehydration device according to Claims 2 or 3, it is characterised in that：The regenerator (5) Side wall top is provided with stripping gas N(2)Inlet tube (5.3), the stripping gas N(2)Inlet tube (5.3) lower section is heater (4) And the pipeline between regenerator (5)；Regenerator (5) bottom is connected with regenerator reboiler (5.1), and regenerator reboiler (5.1) connected with poor rich liquid heat exchanger (3) lower wall other end again, the regenerator reboiler (5.1) and regenerator (5) opposite side Wall lower section connection, regenerator (5) upper end is connected with regenerator condenser (5.2), the regenerator condenser (5.2) with again Raw tower (5) opposite side wall top connection.
5. the oxygen rich fuel gas flue gas TEG dehydration device according to Claims 2 or 3, it is characterised in that the absorption tower (1) Tower diameter size is related to the volume flow of the density, oxygen rich fuel gas smoke density and oxygen rich fuel gas flue gas of glycol solution, and optimization is inhaled The tower diameter size of tower 1 is received, equation below is met：
V=0.0508 [(ρl-ρg)/ρg]0.5 (1-1)
A = Q v - - - ( 1 - 2 )
D = 4 &times; A / &pi; - - - ( 1 - 3 )
ρ in formulalIt is the density of glycol solution, unit is kg/m3；ρgIt is oxygen rich fuel gas smoke density, unit is kg/m3；D is absorption Tower tower diameter, unit is m；Q is the volume flow of oxygen rich fuel gas flue gas, and unit is m3/s；A is absorbing tower plate suqare.
6. oxygen rich fuel gas flue gas TEG dehydration device according to claim 5, it is characterised in that the absorption tower (1) is Plate column, the height of absorption tower (1) is by body height H1, headroom height H2With bottom space height H3Three parts constitute, its In,
Body height H1It is, from tower top ground floor column plate to the vertical range between last layer of column plate of bottom of towe, to be counted according to formula (1-4) Draw：
H1=(N-2-S) × HT+S×H'T+Hf (1-4)
H in formulaTIt is column plate spacing, unit is m；H'TTo be provided with the column plate spacing of manhole, unit is m；S is people's number of perforations, is not wrapped Include the manhole in tower top space and bottom of towe space；HfIt is the spatial altitude of feed zone, unit is m；N is the number of plates；
Headroom height H2Calculating formula such as formula (1-5) shown in：
H2=0.35 × D+1.5 × HT+HC (1-5)
D is tower diameter in formula, and unit is m；HCFor demister highly, unit is m,
Bottom space height H3Calculated according to glycol internal circulating load and tower diameter, as shown in formula (1-6),
H 3 = 4 M &pi;D 2 - - - ( 1 - 6 )
In formula, M is poor triethylene glycol internal circulating load, and unit is m3/ s, π are pi, and D is absorption tower tower diameter, and unit is m.
7. oxygen rich fuel gas flue gas TEG dehydration device according to claim 6, it is characterised in that the absorption tower (1) Column plate stream forms are selected：
As absorption tower tower diameter D≤2.2m, the column plate stream forms use single overflow type；And downflow weir is long in absorption tower (1) Degree L=(0.6~0.8) D,
Or, as absorption tower tower diameter D>During 2.2m, the column plate stream forms are typically using overflow in double overflow type, and absorption tower 1 Weir length L=(0.5~0.7) D；
Height of weir plate is tower clear liquid height on plate H in absorption tower 1aSubtract weir supernatant layer height Hb, i.e. H=Ha-Hb。
8. oxygen rich fuel gas flue gas TEG dehydration device according to claim 7, it is characterised in that the absorption tower (1) Downspout parameter is as follows
Table downspout parameter
Bottom gap (mm) Top width (mm) Bottom width (mm) Straight section height (mm) 30~50 220~260 200~240 180~220
Valve plate structure design
(1) valve opening gas velocity
Valve opening gas velocity on column plate during all float valve standard-sized sheets is referred to as valve hole critical gas-velocity, valve hole critical gas-velocity UcrCalculating formula such as formula Shown in (1-7),
U c r = 1.13 ( H b + 0.5 H ) &Delta; &rho; + 43.35 &rho; g - - - ( 1 - 7 )
H in formulabFor flat weir supernatant layer highly, unit is m；H is height of weir plate, and unit is m；△ ρ are the phase density of air-liquid two Difference, unit is kg/m3；
Float valve number
N 1 = V 1 0.785 U 0 d 0 2 - - - ( 1 - 8 )
V in formula1It is absorption tower gas load, unit is m3/s；U0It is operation valve opening gas velocity, d0It is valve opening diameter, the regenerator Reboiler (5.1) temperature is 188~200 DEG C.
9. a kind of technique of oxygen rich fuel gas flue gas TEG dehydration device, it is characterised in that：Comprise the following steps：
1) poor triethylene glycol enters absorption tower (1) by poor triethylene glycol inlet tube (1.3) through absorption tower (1) top, meanwhile, oxygen-enriched combustion Gas flue gas enters absorption tower (1) by oxygen rich fuel gas smoke air inlet (1.4) through absorption tower (1) bottom；In high pressure normal temperature condition Under, poor triethylene glycol is contacted with the oxygen rich fuel gas flue gas of adverse current, obtains containing CO2Dry gas and rich triethylene glycol；
2) rich triethylene glycol is heated after exiting into check-valves (2) by absorption tower (1) bottom of towe by poor rich liquid heat exchanger (3), is obtained To the elevated rich triethylene glycol of temperature, then rich triethylene glycol is heated in 148 DEG C of entrance regenerator (5) by heater (4), in height Under warm lower pressure, by stripping gas N2The N that inlet tube (5.3) enters2Rich triethylene glycol is stripped, obtain poor triethylene glycol and Vapor, vapor entered regenerator condenser (5.2) discharge, and water steam enters in regenerator (5) after partial liquefaction；
3) poor triethylene glycol is by regenerator reboiler (5.1), regenerated and poor triethylene glycol of the concentration higher than 99%, vaporization it is poor Triethylene glycol and vapor；The poor triethylene glycol and water steam of vaporization enter in regenerator (5)；
4) the poor triethylene glycol of regeneration and concentration higher than 99% is back to poor rich liquid heat exchanger (3), and the regeneration poor three for being cooled down is sweet Alcohol；
5) step 1) in during the dry gas that obtains exits into dry gas-lean solution heat exchanger (7) through absorption tower (1) tower top, while cooling The pressurization of regeneration poor triethylene glycol enter in dry gas-lean solution heat exchanger (7), dry gas carries out heat friendship with the poor triethylene glycol of regeneration of cooling Change, then obtain the poor triethylene glycol that temperature is 35~45 DEG C through the first condenser (8) cooling, and circulation profit is reclaimed with pipeline discharge With the dry gas of heat exchange enters liquefying plant (10) after being cooled down through the second condenser (9), obtains by CO2、N2And O2What is constituted is mixed Gas and water are closed, water is discharged by liquefying plant (10) bottom pipe；
6) gaseous mixture enters separator (11) by liquefying plant (10) top, obtains N2And O2Arranged from separator (11) top Go out, CO of the concentration more than 95%2From the outflow of separator (11) bottom.
10. the technique of oxygen rich fuel gas flue gas TEG dehydration device according to claim 9, it is characterised in that：The step 1) in, the mass fraction of poor triethylene glycol is 99.8%, temperature is 35~45 DEG C, volume flow is 33m3/h；
The step 1) in, oxygen rich fuel gas flue-gas temperature is 35~45 DEG C.
The step 2) in, N2Temperature for 55~65 DEG C, pressure be 1.5bar, molar flow be 50kmol/h.
CN201611058845.1A 2016-11-25 2016-11-25 Triethylene glycol dehydration device and process for oxygen-enriched gas flue gas Pending CN106693617A (en)

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CN110681246A (en) * 2019-07-26 2020-01-14 北京世云科技有限公司 Modified triethylene glycol composition and device for dehumidifying low-concentration gas by using same
CN112742184A (en) * 2021-01-06 2021-05-04 中国石油天然气股份有限公司 Triethylene glycol dehydration device and method for recycling regeneration waste gas
CN113278456A (en) * 2021-06-25 2021-08-20 西南石油大学 Triethylene glycol regenerating unit for pressure boost dehydration station
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CN110681246A (en) * 2019-07-26 2020-01-14 北京世云科技有限公司 Modified triethylene glycol composition and device for dehumidifying low-concentration gas by using same
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CN113278456A (en) * 2021-06-25 2021-08-20 西南石油大学 Triethylene glycol regenerating unit for pressure boost dehydration station
RU220430U1 (en) * 2023-07-11 2023-09-13 Федеральное государственное автономное образовательное учреждение высшего образования "Омский государственный технический университет" (ОмГТУ) DEVICE FOR PURIFYING TRIETHYLENE GLYCOL FROM OILS AND HEAVY HYDROCARBONS
CN117643744A (en) * 2024-01-30 2024-03-05 四川凌耘建科技有限公司 Efficient dehydration method and related device for natural gas triethylene glycol
CN117643744B (en) * 2024-01-30 2024-04-16 四川凌耘建科技有限公司 Efficient dehydration method and related device for natural gas triethylene glycol

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