CN106281411B - A kind of catalytic reforming unit combination desalination preserving method - Google Patents

A kind of catalytic reforming unit combination desalination preserving method Download PDF

Info

Publication number
CN106281411B
CN106281411B CN201610651629.1A CN201610651629A CN106281411B CN 106281411 B CN106281411 B CN 106281411B CN 201610651629 A CN201610651629 A CN 201610651629A CN 106281411 B CN106281411 B CN 106281411B
Authority
CN
China
Prior art keywords
water
dehydration
tower
tank
desalting device
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201610651629.1A
Other languages
Chinese (zh)
Other versions
CN106281411A (en
Inventor
杨强
许萧
卢浩
竺嘉斌
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
East China University of Science and Technology
Original Assignee
East China University of Science and Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by East China University of Science and Technology filed Critical East China University of Science and Technology
Priority to CN201610651629.1A priority Critical patent/CN106281411B/en
Publication of CN106281411A publication Critical patent/CN106281411A/en
Application granted granted Critical
Publication of CN106281411B publication Critical patent/CN106281411B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • 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
    • 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
    • B01D53/261—Drying gases or vapours by adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/406—Ammonia

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present invention relates to catalytic reforming units to combine desalination preserving method, is that dehydration dechlorination tank (7) is added after stabilizer Feed Pressurization pumps (6), water content is less than or equal to 15ug/g after the dehydration dechlorination tank dehydration, and chlorinty is less than or equal to 0.5ug/g；It returns and is added in tower reflux process water-washing desalting device (5) in tower top liquefied gas, the water-washing desalting device (5) largely removes NH3, H2S, HCl inorganic matter, is down to reflux total salt content within 1mg/L.Realize catalytic reforming unit long-period stable operation.

Description

A kind of catalytic reforming unit combination desalination preserving method
Technical field
The present invention relates to catalytic reforming units to combine desalination preserving method, in particular, being related to a kind of for catalysis weight Corrode the combination desalination anti-corrosion method with the more serious stabilizer of salt crust (or depentanizer) in engagement positions, and to catalysis Similar tower class is equally transformed in reformation, realizes catalytic reforming unit long-period stable operation.
Background technique
Catalytic reforming can be used for producing high-knock rating gasoline blend component, can be used for production aromatic hydrocarbons, can also be Various hydrogenation plants provide cheap hydrogen.It with oil property change weight, deteriorates, environmental requirement is continuously improved, catalytic reforming process Good development prospect is encountered, process scale is gradually expanded.
Catalytic reforming reaction product liquid is sent to stabilizer (or depentanizer), and stabilizer upper product is C5-, tower bottom Product is C6+.Stablize overhead gas and enter return tank after condensing, tank deck goes out fuel gas.Tank bottom goes out liquefied gas, and a part is returned Stream, a part do product.
The common salt crust phenomenon of stabilizer (or depentanizer) top tray, overhead gas condensing heat exchanger block up frequent occurrence Plug.What is come along with salt crust is serious corrosion, seriously endangers safety and steady production, the catalytic reforming of most domestic is all It is faced with corrosion and the puzzlement of salt crust.Salt crust and the principal element of corrosion are as follows:
The source of chlorine: (1) chemical assistant for improving crude oil recovery ratio in oil recovery process is added, leads to chloride in naphtha Impurity increases.(2) it in order to keep the acid function of dual metal reforming catalyst, needs to carry out catalyst continuous to mend chlorine, catalysis The chlorine being lost in agent enters stabilizer with reaction product.
The source of water: reforming catalyst need to carry out water chloride balance control, be needed in reaction atmosphere containing suitable water, but anti- Stabilizer should be entered afterwards does not have mating suitable dehydration facility, is stablizing tower top, and hydrogen chloride forms hydrochloric acid after meeting water, produces to equipment Raw strong corrosiveness.
The source of nitrogen: reformer feed generally comprises straight-run naphtha, hydrocracked naphtha, coking naphtha, catalysis are split Naphtha, cracking of ethylene naphtha, which are raffinated oil etc., wherein contains considerable amount of nitrogen.Pre-add before most of reforming reaction The denitrification activity of hydrogen catalyst weakens with the time, causes nitrogen to enter reforming reaction and generates NH3。
The source of sulphur: in addition to the micro element sulphur of reformer feed entrainment, in reforming reaction, using sulphur to reforming catalyst Active deactivation limits certain catalyst and goes into operation overheating problem, infuses sulphur in catalyst bed, completes pre-vulcanization process.One As require in reaction raw materials sulfur content to be not less than 0.2 μ g/g.
Salt crust and corrosion have compared with other devices and process at the top of catalytic reforming unit stabilizer (or depentanizer) The characteristics of having oneself and reformer is anticorrosive in the process of running and the focal point of resistive connection salt.
After the inorganic constituents such as the chlorine of reforming reaction, nitrogen, sulphur enter fractionating system, corrosion and salt crust are formed.Corrode Because in HCl-H2S-H2O system, HCl and H2S mutually promotes, and to constitute cyclic corrosion even more serious, and this system is adding water dilute Still there is very strong corrosive power after releasing, can not be solved by straight waterflooding.
Salt crust is due to NH3The ammonium salt and FeCl that HCl is formed2The crystallization of equal compounds.By enhancing pre- hydrogenation catalyst The denitrification ability of agent can not completely eliminate salt crust, illustrate FeCl2It crystallizes Deng the compound generated due to corrosion in salt crust process In also take up a part of reason.
Solving catalytic reforming unit stabilizer (or depentanizer) top tray salt crust and corrosion fundamental requirement is simultaneously Solve salt crust and corrosion.
On some reformers, debutanizing tower, dehexanizer, pre-add hydrogen stripper similarly there is tower top salt crust and Corrosion, the reason is that since compounds such as chlorine, sulphur, nitrogen are converted salt crust and corrosive medium and reformer by hydrogenation reaction Anticorrosive in the process of running and resistive connection salt one of focus.
In order to resist above-mentioned corrosion and salt crust, sulphur, chlorine, nitrogen in strict control raw material contain catalytic reforming process units at present Amount, enhances the denitrification ability of raw material catalyst for pre-hydrogenation, controls the water chloride balance of reforming catalyst emphatically in technique.This Solution is started with from process optimization angle, and operating flexibility is small and implements complexity, still without being directed to salt crust and corrosion location Carry out the solution of essence.
Operation scheme is also periodically rinsed salt crust pipeline at present, or add and fill the water in the process of top/cut water Tank.But water injection extraction is inefficient, inorganic salt impurities cannot obtain efficient removal；The tower hydro carbons that returns after cutting water is easy to make liquid Water brings tower bottom into；The water entrainment hydro carbons cut out simultaneously, causes water process difficulty and hydro carbons to waste.
Common also fills the water at tower charging, although tower top salt crust can be solved the problems, such as temporarily, charging water filling adds The acute chlorine corrosion of equipment, is not a very perfect processing method.The above method is all not ideal enough.
Summary of the invention
The present invention provides a kind of catalytic reforming units to combine desalination preserving method, is effectively relieved and reduces catalytic reforming Salt crust and corrosion at the top of device stabilizer, and tower class similar in catalytic reforming is equally transformed, realize catalytic reforming dress Set long-period stable operation.
A kind of catalytic reforming unit combination desalination preserving method is to add dehydration after stabilizer Feed Pressurization pumps (6) Dechlorination tank (7), water content is less than or equal to 15ug/g after the dehydration dechlorination tank dehydration, and chlorinty is less than or equal to 0.5ug/g；In tower Top liquefied gas is returned and is added in tower reflux process water-washing desalting device (5), and the water-washing desalting device (5) is by NH3, H2S, HCl inorganic matter A large amount of removings are down to reflux total salt content within 1mg/L.
In a preferred embodiment, three moulds are adsorbed in the dehydration of dehydration dechlorination tank (7) built-in fabric, molecular sieve water suction, dechlorination Block adsorbs three steps through fiber dehydration, molecular sieve dehydration, dechlorination into tower raw material.Fiber dewatering module most of can will dissociate Water separation reduces molecular sieve water suction total amount in the unit time, extends the molecular sieve replacement cycle.Dechlorination adsorbent can be with Ca, Na or Al is the antichlor of active component.
In another preferred embodiment, the dehydration of dehydration dechlorination tank (7) built-in fabric is 316 wires of 0.5mm using string diameter It being woven with the Teflon fiber combinations of string diameter 0.4mm, braiding voidage is 60%, Residence Time 15 seconds.
In another preferred embodiment, efficient water-washing desalting device (5) includes water filling distribution, axis stream extracts, modified fibre takes off Three modules of water.Water filling distribution makes the demineralized water of injection or boiler (III) realize and be evenly distributed in returning tower withdrawing oil；Axis stream extraction The rotation of water droplet high speed and revolution for realizing near-spherical are taken, and keeps drop particle diameter uniform to about 5-10 μm；Efficient water-washing desalting device (5) drop particle diameter can be totally removed in 3 μm or more of moisture for modified fibre dewatering module, be using fibrous material Teflon, Nylon, PP, 316L, modification mode are that capillary is modified, by control fiber string diameter (size 12 ~ 120 μm it Between) to the capillary force of water droplet, three control parameters of modified fibre bed include residence time (20 ~ 40 seconds), liquid for acquisition Drip superficial velocity (0.005 ~ 0.018m/s), voidage (40% ~ 50%).The partial size control being dehydrated by water injection extraction and modified fibre Process processed realizes the optimization coupling of extraction and dehydration, as far as possible without water filling impurely to returning the sepatation etching of tower withdrawing oil and salt crust Medium.
In another preferred embodiment, still needs to consider to return in tower reflux under maximum conditions in tower top and carries portion of water secretly, Prevent liquid water from entering tower bottom, the control of stripping section temperature is under partial pressure more than water vapour dew point.
In another preferred embodiment, efficient water-washing desalting device (5) water injection rate (v/v) is mix oil plant (VI) flow 2% ~ 10%(v/v).
In another preferred embodiment, efficient water-washing desalting device (5) axis stream extraction is flowed using axial admission radial rotary Extraction core pipe, core pipe using Parallel Design reach treating capacity requirement, core pipe diameter optional 20mm, 40mm, 70mm are respectively corresponded Axial admission flow velocity be 2.5m/s, 4m/s, 6m/s.
In another preferred embodiment, efficient water-washing desalting device (5) includes the sleeping tank of the sleeping tank in top and lower part.The top is sleeping Tank includes built-in axis stream extraction core pipe and built-in modifying and dewatering fiber, top crouch tank diameter with coutroi velocity 0.005 ~ 0.018m/s is reference parameter.Crouch water oil removing built-in fabric built in tank for lower part, and the oil content for brackish water of going out is not more than 150ppm (petroleum content).
Detailed description of the invention
Fig. 1 is the combination desalination anti-corrosion for catalytic reforming unit depentanizer according to embodiment of the present invention Flow diagram.
I-fixed gas, II-pentane go out, and III-demineralized water or boiler water, IV-brackish water go out, and V-de- pentane product goes out, and VI- Mix supplied materials
1- stabilizer (or depentanizer), 2- condensing heat exchanger, 3- return tank of top of the tower, 4- overhead reflux booster pump, 5- Efficient water-washing desalting device, 6- mixing supplied materials booster pump, 7- supplied materials are dehydrated dechlorination tank, 8- tower bottom heat exchanger, the reflux pressurization of 9- tower bottom Pump, 10- tower bottom reboiler furnace
The mixing oil plant (VI) that upstream is come is pressurized through feed pump (6), into dehydration dechlorination tank (7) removing traces of moisture and chlorine Compound, material enter tower (1) after tower bottom heat exchanger (8), and it is laggard that tower bottom product part overhead product enters condensing heat exchanger (2) Enter return tank of top of the tower (3), is the fixed gas (I) containing C3, C4, the liquefaction of return tank of top of the tower (3) bottom at the top of return tank of top of the tower (3) Gas is pumped (4) pressurization a part and is sent outside as product, and a part returns tower and realizes reflux operation, returns the liquefied gas of tower reflux through excessively high The inorganic salts and moisture for imitating water-washing desalting device (5) removing entrainment, gradually decrease overhead reflux system salt content and corrosion rate.
Specific embodiment
The present inventor's discovery later after extensive and in-depth study, reformer depentanizer overhead reflux temperature About 40 DEG C of degree has liquid water generation due to the inhomogeneities of heat transfer lower than vapor dew-point temperature, dissolves in gas phase rapidly NH3, H2S and HCl form HCl-H2S-H2O corrosion system and NH4Cl salt crust system.Depentanizer tower tray salification, influences tower Mass transfer, heat-transfer effect, separation accuracy is inadequate, or even causes liquid flooding.Salt crust ingredient is mainly ammonium chloride, there are also part iron rust, is urged The particles such as agent, while exacerbating the underdeposit corrosion of equipment.
The method that domestic catalytic reforming unit generallys use online water filling cleaning.It on the one hand is the place note in ammonium salt blockage Water, such as tower top air cooler, tower top booster pump, tower top tower tray etc..It on the other hand is filled the water at tower raw material.Similar shut-down It fills the water and brings safety problem to normal production, reduce economical operation benefit；Also there is the case filled the water online, although online note Salt crust phenomenon is alleviated after water, but tower tray, the corrosion of overhead reflux system are more violent after filling the water, concern when also taking Stripping section temperature, prevents liquid water to be entrained into tower bottom.
The condition that the flow morphology of axial admission radial rotary provides efficient mass transfer and quickly spread for extraction, compared to The method that a kind of spiral-flow type of Chinese patent ZL 201310556596.9 strengthens absorption heavy metal ion, axial admission radial rotary Fluidised form is that eddy flow micro turbulence improves and optimizes, and abandons its Separation Indexes reached using density contrast, but borrows its reinforcing The characteristic of absorption and mass transfer, to realize that depth extraction process, the inorganic matters such as NH3, H2S, HCl are diffused into the diffusion of water droplet from oil Rate is strengthened.Wherein for the application in this field, about the centrifugation radius (core pipe diameter) of dead axle stream extraction and charging are needed Flow velocity.
In conjunction with advanced polymer material science, the coarse separation of modified fibre is common in nearest Chinese patent ZL 201410211201.6, ZL 201410211202, ZL 201410210930.X, 201410210965.3 ZL etc. describe fibre Dimension coalescence is used for oil water separation process, long service life, without secondary pollution, in depentanizer charging dehydration and depentanizer reflux Oily dehydration is dehydrated using fiber dehydration and modified fibre respectively, we need to control the production material of fiber dehydration, gap Rate, residence time and superficial velocity, to meet the dehydration indexes under this working condition.
The present invention provides a kind of catalytic reforming units to combine desalination preserving method, is effectively relieved and reduces catalytic reforming Salt crust and corrosion at the top of device stabilizer (or depentanizer), and tower class similar in catalytic reforming is equally transformed, Realize catalytic reforming unit long-period stable operation.It includes that following two step (is with depentanizer combination desalination anti-corrosion Example):
(1) dehydration dechlorination tank (7) is added after Feed Pressurization pump (6), built-in mixing supplied materials fiber dewatering module, molecular sieve are inhaled Water module and dechlorination adsorption module, water content is less than or equal to 15ug/g after dehydration dechlorination tank dehydration, and chlorinty is less than or equal to 0.5ug/g。
(2) return that efficient water-washing desalting device (5) is added in tower reflux process is inorganic by NH3, H2S, HCl etc. in tower top liquefied gas Object largely removes, and is down to reflux total salt content within 1mg/L.
In a preferred embodiment, three moulds are adsorbed in the dehydration of dehydration dechlorination tank (7) built-in fabric, molecular sieve water suction, dechlorination Block adsorbs three steps through fiber dehydration, molecular sieve dehydration, dechlorination into tower raw material.Fiber dewatering module most of can will dissociate Water separation reduces molecular sieve water suction total amount in the unit time, extends the molecular sieve replacement cycle.Dechlorination adsorbent can be with Ca, Na, Al are the antichlor of active component.
In another preferred embodiment, the dehydration of dehydration dechlorination tank (7) built-in fabric is 316 wires of 0.5mm using string diameter It being woven with the Teflon fiber combinations of string diameter 0.4mm, braiding voidage is 60%, Residence Time 15 seconds.
In another preferred embodiment, efficient water-washing desalting device (5) includes water filling distribution, axis stream extracts, modified fibre takes off Three modules of water.Water filling distribution makes the demineralized water of injection or boiler (III) realize and be evenly distributed in returning tower withdrawing oil；Axis stream extraction The rotation of water droplet high speed and revolution for realizing near-spherical are taken, and keeps drop particle diameter uniform to about 5-10 μm；Efficient water-washing desalting device (5) drop particle diameter can be totally removed in 3 μm or more of moisture for modified fibre dewatering module, be using fibrous material Teflon, Nylon, PP, 316L, modification mode is modified for capillary, and the capillarity to water droplet is obtained by control fiber string diameter Power, three control parameters of modified fibre bed include residence time (20 ~ 40 seconds), drop superficial velocity (0.005 ~ 0.018m/ S), voidage (40% ~ 50%).The size controlling process being dehydrated by water injection extraction and modified fibre, realization extraction and dehydration Optimization coupling, as far as possible without water filling impurely to returning the sepatation etching of tower withdrawing oil and salt crust medium.
In another preferred embodiment, still needs to consider to return in tower reflux under maximum conditions in tower top and carries portion of water secretly, Prevent liquid water from entering tower bottom, the control of stripping section temperature is under partial pressure more than water vapour dew point.
In another preferred embodiment, efficient water-washing desalting device (5) water injection rate (v/v) is mix oil plant (VI) flow 2% ~ 10%(v/v).
In another preferred embodiment, efficient water-washing desalting device (5) axis stream extraction is flowed using axial admission radial rotary Extraction core pipe, core pipe using Parallel Design reach treating capacity requirement, core pipe diameter optional 20mm, 40mm, 70mm are respectively corresponded Axial admission flow velocity be 2.5m/s, 4m/s, 6m/s.
In another preferred embodiment, efficient water-washing desalting device (5) includes the sleeping tank of the sleeping tank in top and lower part.The top is sleeping Tank includes built-in axis stream extraction core pipe and built-in modifying and dewatering fiber, top crouch tank diameter with coutroi velocity 0.005 ~ 0.018m/s is reference parameter.Crouch water oil removing built-in fabric built in tank for lower part, and the oil content for brackish water of going out is not more than 150ppm (petroleum content).
The major advantage of method of the invention is:
1, high to the mixing supplied materials dehydration into tower, dechlorination efficiency, normal produce of tower is not influenced, effectively control into The Control of Impurities of tower, from control total impurities content on the supplied materials source that tower operates.
2, overhead reflux is efficiently washed and is separated (extraction/separation) and make corrosion and salt crust medium content in overhead system It gradually decreases, and the water injected obtains effectively stable removing, water injection rate is controllably in minimum zone.
3, former overhead reflux temperature is at 40 DEG C or so, and in increasing after efficient water-washing desalting device (5), overhead reflux temperature is about 35 DEG C, on overhead reflux normal operating substantially without influence.
3, corrosion and the more serious stabilizer of salt crust (or depentanizer) in catalytic reforming unit, debutanizing tower, de- All there is same problem in hexane tower, pre-add hydrogen stripper, improved catalytic reforming operation eliminates the puzzlement of corrosion and salt crust.
4, entrainment hydro carbons is less than 150ppm(petroleum-type in the brackish water after the completion of filling the water), reduce water process difficulty and hydro carbons Waste.
5, combination desalination preserving method is a set of to set for catalytic reforming unit stabilizer (or depentanizer) is special Fixed operating parameter system, had both embodied raw material process control, had also done specific aim processing to salt crust seriously corroded position, and There is no the increase of extra power energy consumption.Meanwhile also identifying the separation of this method and the marked improvement of extraction step.
Below with reference to specific embodiment, the present invention is further explained.It should be appreciated, however, that these embodiments are only used for It is bright the present invention and be not meant to limit the scope of the invention.In the following examples, the experimental methods for specific conditions are not specified, usually According to normal conditions, or according to the normal condition proposed by manufacturer.Unless otherwise indicated, all percentage and number be by weight Meter.
Embodiment
Certain domestic 1,200,000 tons/year of continuous reformer reform de- pentane and operate extremely unstable, tower top pressure discontinuity wave It is dynamic, temperature malfunction, sensitive plate temperature by 130~135 DEG C of fluctuations under normal circumstances to 100~160 DEG C, column bottom temperature 205~208 DEG C are down to by normal 212 ± 2 DEG C, C4 the and C5 content in tower bottom reformed oil continues exceeded.According to this hair Bright method adds dehydration dechlorination tank after depentanizer Feed Pressurization pump, returns in tower top liquefied gas and adds height in tower reflux process Imitate water-washing desalting device.
(1) depentanizer feed rate 110t/h, 147 DEG C of inlet temperature of stabilizer, tower top pressure 0.85MPa, overhead reflux oil stream Measure 25t/h.
(2) being dehydrated dechlorination tank is sleeping tank, and diameter of phi 2000mm, length of tangent line 4000m, one opens standby, a mixing supplied materials dehydration fibre Thickness degree 300mm is tieed up, molecular sieve water absorbing agent uses 4A molecular sieve, and antichlor is Ca based dechlorinating agent.
(3) efficiently water-washing desalting device is the sleeping tank of upper and lower level, and the tank diameter that often crouches is 800mm, and built-in axis stream extraction core pipe is straight Diameter is 25mm, and built-in withdrawing oil dehydrated fiber is with a thickness of 200mm.
Injecting desalination water flow in efficient water-washing desalting device in implementation process is 1t/h, and the brackish water of removing enters at sewage Manage device.
Result of implementation discovery, after transformation comes into operation three days, reformer depentanizer tower top pressure restores normal, temperature control Restore normal.After transformation comes into operation three months, check that overhead reflux system eliminates salt crust situation, equipment is without obvious corrosion.
From in above-described embodiment it can clearly be seen that the present invention efficiently solves in catalytic reforming unit corrosion and salt crust ratio More serious stabilizer (or depentanizer), debutanizing tower, dehexanizer, pre-add hydrogen stripper corrode salt crust problem, enhance Tolerance of the catalytic reforming unit to corrosion and salt crust medium.

Claims (5)

  1. It is to add dehydration after stabilizer Feed Pressurization pumps (6) to take off 1. a kind of catalytic reforming unit combines desalination preserving method Chlorine tank (7), water content is less than or equal to 15ug/g after the dehydration dechlorination tank dehydration, and chlorinty is less than or equal to 0.5ug/g；In tower top Liquefied gas returns and adds efficient water-washing desalting device (5) in tower reflux process, and the efficient water-washing desalting device (5) is by NH3、H2S, HCl without Machine object largely removes, and is down to reflux total salt content within 1mg/L；
    Three modules are adsorbed in dehydration dechlorination tank (7) the built-in fabric dehydration, molecular sieve water suction, dechlorination；The molecular sieve water suction Using 4A molecular sieve, dechlorination adsorbent is the antichlor using Ca, Na or Al as active component；
    Dehydration dechlorination tank (7) the built-in fabric dehydration uses 316 wires and string diameter 0.4mm that string diameter is 0.5mm Teflon fiber combinations braiding, braiding voidage be 60%, Residence Time 15 seconds；
    The efficient water-washing desalting device (5) includes water filling distribution, the extraction of axis stream, modified fibre three modules of dehydration；
    The water filling distribution module makes the demineralized water of injection or boiler water (III) realize and be evenly distributed in returning tower withdrawing oil, water droplet 5-10 μm of partial size；Axis stream extraction module realizes the rotation of water droplet high speed and revolution of near-spherical, and rotational velocity range is 2000 ~ 6000r/min, revolution speed range are 200 ~ 1000r/min；Water of the modified fibre dewatering module by drop particle diameter at 3 μm or more Divide and be totally removed, the use of fibrous material is Teflon, Nylon, PP, 316L, modification mode is modified for capillary, passes through and controls fiber String diameter obtains the capillary force to water droplet, and fiber diameter size range is 12 ~ 120 μm, the residence time of modified fibre bed It is 40% ~ 50% that range, which is 20 ~ 40 seconds, drop superficial velocity range is the .018m/s of 0 .005 ~ 0, voidage range.
  2. 2. the method as described in claim 1 carries portion of water secretly if returning in tower reflux in tower top, to prevent liquid water from entering Tower bottom, the control of stripping section temperature is under partial pressure more than water vapour dew point.
  3. 3. the method as described in claim 1, efficient water-washing desalting device (5) water injection rate is mix oil plant (VI) flow 2% ~10%；In overhead reflux 0.1 ~ 1mg/L of salt content, water injection rate 2%；In overhead reflux 1 ~ 5mg/L of salt content, water injection rate It is 6%；When overhead reflux salt content is greater than 5mg/L, water injection rate 10%.
  4. 4. the method as described in claim 1, efficient water-washing desalting device (5) the axis stream extraction uses axial admission radial rotary The extraction core pipe of flowing, core pipe reach treating capacity requirement using Parallel Design, and core pipe diameter selects 20mm, 40mm, 70mm, right respectively The axial admission flow velocity answered is 2.5m/s, 4m/s, 6m/s.
  5. 5. the method as described in claim 1, the efficient water-washing desalting device (5) includes the sleeping tank of the sleeping tank in top and lower part；It is described The top tank that crouches includes built-in axis stream extraction core pipe and built-in modifying and dewatering fiber, top crouch tank diameter with coutroi velocity 0.005 ~ 0.018m/s；Crouch water oil removing built-in fabric built in tank for lower part, and the oil content for brackish water of going out is not more than 150ppm.
CN201610651629.1A 2016-08-11 2016-08-11 A kind of catalytic reforming unit combination desalination preserving method Active CN106281411B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610651629.1A CN106281411B (en) 2016-08-11 2016-08-11 A kind of catalytic reforming unit combination desalination preserving method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610651629.1A CN106281411B (en) 2016-08-11 2016-08-11 A kind of catalytic reforming unit combination desalination preserving method

Publications (2)

Publication Number Publication Date
CN106281411A CN106281411A (en) 2017-01-04
CN106281411B true CN106281411B (en) 2018-12-28

Family

ID=57667857

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610651629.1A Active CN106281411B (en) 2016-08-11 2016-08-11 A kind of catalytic reforming unit combination desalination preserving method

Country Status (1)

Country Link
CN (1) CN106281411B (en)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109652118B (en) 2017-10-10 2020-07-07 中国石油化工股份有限公司 Washing desalination and oil-water separation process system and process method
CN108654376A (en) * 2018-04-18 2018-10-16 陕西未来能源化工有限公司 The recovery system and its method of ammonia in a kind of novel desulphurization solution
CN112779046B (en) * 2020-11-06 2022-07-05 中国石油天然气股份有限公司 Device and method for preventing salt deposition corrosion of stripping tower of oil refining device

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4269694A (en) * 1979-10-01 1981-05-26 Phillips Petroleum Company Method of removing contaminant from a feedstock stream
PT1298185E (en) * 2001-09-27 2005-08-31 Kurita Europ Gmbh METHOD TO PREVENT INCRUSTACTIONS AND CORROSION CAUSED BY AMMONIUM CHLORIDE
CN104711008B (en) * 2015-03-12 2017-12-22 中国石油化工股份有限公司 A kind of device for preventing oil distillation column salt crust

Also Published As

Publication number Publication date
CN106281411A (en) 2017-01-04

Similar Documents

Publication Publication Date Title
CN106281411B (en) A kind of catalytic reforming unit combination desalination preserving method
US20110089013A1 (en) Apparatus of produced water treatment, system and method of using the apparatus, and method of water reuse by using the same
EP3025771B1 (en) Method for removal of hydrogen sulfide from geothermal steam and condensate
Yang et al. Simulation and operation cost estimate for phenol extraction and solvent recovery process of coal-gasification wastewater
CN104826455B (en) Method using ionic liquid for gas drying and dehydration
CN102642881A (en) Device and method for steam stripping of condensate in water gas conversion process
CN104151119A (en) Method for preparing isooctane by deep processing of n-butane
CN111656113A (en) Apparatus and process for removing carbon dioxide from gas streams and treating brine/wastewater from oil fields
CN104704084B (en) Process for washing a gas from a hydroprocessed effluent, and an apparatus and separator relating thereto
CN101376550B (en) Method for processing process waste water of dimethyl ether preparation by dehydrating methyl alcohol
CN109666508B (en) Transformation method for improving economic operation period of hydrogenation device
KR20190104050A (en) Power generation system and process
CN107699273A (en) A kind of anhydrous atmospheric and vacuum distillation technique and device
CN204151297U (en) A kind of chlorion extracting corrosion-resisting device
CN214115234U (en) Desalting system for salt-containing organic wastewater
CN109929638A (en) A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method
CN109534569A (en) Handle method and apparatus for carrying out the method system containing sour ammonia-containing water
CN105964004B (en) A kind of sulfuric acid alkylation reaction product asks for the device of flash evaporation
CN107177372A (en) The suspended bed hydrogenation method and hydrogenation system of heavy oil feedstock
CN102167412A (en) High-efficiency composite urea waste liquid deep hydrolysis desorption tower
CN104645811B (en) Device for recovering tail gas and recovery process thereof
CN204469528U (en) Device for recovering tail gas
CN210462963U (en) Dilute steam generator capable of controlling steam/hydrocarbon ratio for light hydrocarbon thermal cracking
CN206706040U (en) A kind of ammonia nitrogen removal device based on integral gasification combined circulation technology gas gasification and desulfurization unit
CN202186948U (en) Technical steam generating system suitable for technology of preparing propylene by coal-based methanol

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant