CN209396928U - A kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling - Google Patents
A kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling Download PDFInfo
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- CN209396928U CN209396928U CN201920050249.1U CN201920050249U CN209396928U CN 209396928 U CN209396928 U CN 209396928U CN 201920050249 U CN201920050249 U CN 201920050249U CN 209396928 U CN209396928 U CN 209396928U
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Abstract
The utility model discloses the processing units of a kind of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling, comprising: pre-concentration unit, for carrying out the processing of multiple-effect evaporation pre-concentration to catalytic cracking unit desulfurization wastewater, so that the Na of the concentrate after concentration2SO4Mass concentration is 20-40%, and temperature is 60-80 DEG C, and the concentrate after pre-concentration is sent into spray drying unit；It is spray-dried unit, for crystallization to be dried using flue gas to the concentrate after multiple-effect evaporation pre-concentration, the utility model is by multiple-effect evaporation and is spray-dried the combination of two kinds of technique, it can be achieved that the purpose handled catalytic cracking unit desulfurization wastewater.
Description
Technical field
The utility model relates to the technical fields of desulfurization wastewater processing, more particularly to a kind of catalytic cracking (Fluid
Catalytic Cracking, FCC) device desulfurization wastewater and flue gas thermal coupling processing unit.
Background technique
Currently, the flue gas generated when most of the country catalytic cracking unit catalyst regeneration, contains NOx and SO2, urge
The pollutants such as agent powder.In order to reach discharge standard, it is necessary to carry out desulphurization denitration to regenerated flue gas.
Oil refining enterprise generally uses NaOH as desulfurizing agent, using wet processing, after The Waste Heat Boiler of Catalytic Cracking Units,
Wet desulfuration tower is set, NaOH and Na will be contained2SO3Slurries as absorbent, sprayed into from the top on absorption tower, to from lower
On flue gas washed.SO in the contact process of slurries and flue gas, in flue gas2By the NaOH and Na in slurries2SO3Into
Row chemical reaction, generates Na2SO3And NaHSO3It is absorbed washing to get off, to achieve the purpose that purifying and catalyzing regenerated flue gas.
The slurries of absorb the bottom of the tower, some needs to be discharged absorption tower as desulfurization wastewater, and discharge mode is continuous
's.The waste water on absorption tower is discharged due to containing SO3, it is therefore desirable to it is further aoxidized, to reduce the COD of efflux wastewater
(Chemical Oxygen Demand, COD) value.Oxidation is carried out by way of being passed through air in oxidation tank
, by the Na in waste water in purpose2SO3And NaHSO3It is oxidized to Na2SO4, in order to keep oxidation process pH value to maintain neutrality, need
NaOH to be added in oxidation process to adjust the pH value of waste water.
Oxidized waste water, after the pH value of COD reaches standard, the rear discharge catalytic cracking unit of concentration, Entry Firm
Sewerage enters urban sewage system.
The catalytic cracking and desulfurizing waste water of outlet easily causes to impact, sternly since its salt content is higher to biochemical wastewater treatment
Ghost image rings the normal production in sewage farm, it is therefore desirable to be further processed to it.And the wastewater flow rate of outlet, depend on catalysis again
SO in raw flue gas2Content, regenerated flue gas SO2Content is high, then needs the wastewater flow rate of outlet big.
Currently, the catalysis flue gas desulfurization waste-water of discharge up to standard typically form such as the following table 1 after oxidation:
Table 1
Wherein chloride ion content depends on chlorinity and the total dissolved solidss content of discharge in the raw water of supplement, and floating outstanding object contains
Amount depends on the wastewater flow rate of catalyst powder dust content and outlet in former flue gas.
The desulfurization wastewater in thermal power plant at present has been looked into following several Zero discharge treatment methods:
1, " chemical tendering+evaporative crystallization " desulfurization wastewater technique of zero discharge
By the way that various chemical agents are added, the substance that useless water part is easily crystallized removes the technique, makes multiple-effect evaporation system
Various kinds of equipment, the pipeline of system etc. are less scaling, to ensure that the long-term operation of evaporation equipment.
However, there is also following disadvantages for the technique:
1) this method needs to be added various chemical medicaments, and the cost of processing is relatively high, and part chemical agent enters sewage
System has aggravated the processing load of sewage disposal system；
2) crystallization generally uses evaporation and crystallization mode, and the heat source using steam as heating, i.e. this method leans on steam completely
Heat waste water is evaporated, so steam consumption is larger, operating cost is more expensive；
3) during salt is concentrated, the chlorine ion concentration height of solution and the concentration of salt can be stepped up, so evaporation
And the relevant static equipment of crystallization, conveying machinery, pipeline, valve, measurement and control instrument etc., it is required to using energy high chlorine resistant, height
The construction investment of the Langaloy or titanium steel material of salt, project is high, and maintenance cost is high；
4) the pretreated method of film is used, the consumption of steam can be reduced, but use the time partially short due to film, needed good
Maintenance and replacement, operation it is costly.
2, " fume afterheat flash concentration+flue evaporation " desulfurization wastewater technique of zero discharge
The technology uses multiple-effect evaporation technique, and desulfurization wastewater is carried out pre-concentration, and the salt content in desulfurization wastewater is improved 5
To 10 times.Desulfurization wastewater after pre-concentration is evaporated in the flue for being pumped into boiler.The technology strong brine sprays into cigarette
When road, it is desirable that the temperature of flue gas is greater than 300 DEG C, positioned at the front end of economizer and cleaner.
Strong brine is sprayed into flue collector, is contacted with 300 DEG C or more of high-temperature flue gas, strong brine be heated, evaporate immediately and
Crystallization, high-temperature flue gas synchronous cooling in evaporation process.After the completion of evaporating operation, the mixing of the microparticle of flue gas and crystallization salt
Object enters back into economizer together, and in economizer, high temperature enters economizer together with the microparticle mixture of salt, with air into
Row heat exchange, the flue gas after heat exchange enter cleaner together with dust and salt particle in flue gas, the dust and salt in flue gas
Microparticle is removed in deduster.
However, the technique but has the following disadvantages:
1) desulfurization waste liquor is not evaporated directly, but due to using pre-concentration to the wet process of FGD of calcium carbide by the technique
It is generally 10000 to 20000mg/L from the concentration of the chloride ion of desulphurization system outlet, waste water is through pre- for the waste water discharged
Concentration is concentrated by evaporation to after 5 to 10 times, and the chlorine ion concentration of concentrate is up to 50000 to 100000mg/L, and chloride ion pair
Austenite equipment has extremely strong corrosivity, so, all devices, pipeline, conveying machinery, measuring instrumentss for contacting with concentrate etc. are equal
The Langaloy or titanium alloy material of energy anti-chlorine ion corrosion are needed, equipment investment is larger；
2) waste water after pre-concentration is injected directly into 300 DEG C or more of high temperature flue collector, utilizes high-temperature flue gas by the technique
In heat by concentrate evaporative crystallization.In the evaporation process of flue collector, flue gas needs to provide required for concentrate evaporation
Heat will affect flue gas so main flue gas temperature will reduce 5-8 DEG C --- and the heat exchange efficiency of air economizer reduces air
Charging temperature, to influence the actual efficiency of boiler.On the other hand, salt contained in waste water, is crystallized out in flue collector
Come, in the form of microparticle together with dust, enters economizer with main flue gas.These solid particulate matters, on the one hand to economizer
It will cause corrosion, to reduce the cycle of operation of boiler system, on the other hand, solid particulate matter is easily in the heat exchanger tube for saving cigarette device
Deposition, the biography for reducing province's cigarette device, which is changed, is；
3) since concentrate has extremely strong corrosivity, once concentrate system leak, concentrated liquid is each with flue collector system
Class equipment contact, it will heavy corrosion is caused to flue system, influences the normal operation of boiler.
Utility model content
In order to overcome the deficiencies of the above existing technologies, the utility model is designed to provide a kind of catalytic cracking unit
The processing unit of desulfurization wastewater and flue gas thermal coupling, to realize by the combination of two kinds of technique of multiple-effect evaporation and spray drying
To the purpose of catalytic cracking unit desulfurization wastewater processing.
In order to achieve the above object, the utility model proposes the processing of a kind of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling
Device, comprising:
Pre-concentration unit, for carrying out the processing of multiple-effect evaporation pre-concentration to catalytic cracking unit desulfurization wastewater so that after concentration
The Na2SO4 mass concentration of concentrate be 20-40%, temperature is 60-80 DEG C, and the concentrate after concentration is sent into spraying dry
Dry unit；
It is spray-dried unit, crystallization is dried using flue gas to the concentrate after multiple-effect evaporation pre-concentration.
Preferably, the pre-concentration unit includes:
Multi-effect evaporator system carries out multiple-effect evaporation to the catalytic cracking unit desulfurization wastewater of feeding；
Pumped vacuum systems connects the Multi-effect evaporator system, to reduce the multi-effect evaporator by pumped vacuum systems
The operating pressure of evaporator in system, reduces the operation temperature of evaporator；
Condenser system connects the Multi-effect evaporator system, is steamed with every level-one multiple-effect to the Multi-effect evaporator system
The steam water outlet of hair carries out cooling recycling；
Concentrate removes spraying system, connects the Multi-effect evaporator system, to steam to the Multi-effect evaporator system multiple-effect
Concentrate after hair pre-concentration carries out spraying treatment, and concentrate is sent into spray drying unit by treated.
Preferably, the multiple-effect evaporation medium of the Multi-effect evaporator system, using the condensed water in high temperature in steam or device
Or low temperature position hot water.
Preferably, the operation temperature of the afterbody evaporator of the Multi-effect evaporator system is controlled at 60-80 DEG C.
Preferably, chlorine ions concentration < 3000mg/ of the concentrate after pre-concentration unit multiple-effect evaporation concentration
L。
Preferably, the spray drying unit includes:
Spray drying tower, the spray drying tower include drying tower tower body and atomization system, the desulfurization waste liquor after concentration
After being sent into the spray drying tower, concentrating spent liquor is atomized by the atomization system, concentrating spent liquor is atomized into micro- liquid
It drips, the moisture content in microlayer model is precipitated using the smoke evaporative in spray drying tower, crystallization, and crystal salt particle small part is in the spray
Sedimentation, is discharged by bottom in mist drying tower, most of to be carried by flue gas, is left the spray drying tower and is entered dust removing units；
Dust removing units, for being dusted processing to the flue gas for leaving drying tower, by catalyst dust contained in flue gas
It filters and is recycled together with the salt of crystallization, and the flue gas after dedusting is sent into the absorption tower of wet desulphurization.
Preferably, the atomization system is set to the top of the spray drying tower, by the particle after atomization from the spray
It is sprayed at the top of mist drying tower.
Preferably, the flue gas in the spray drying tower for spray drying is the catalysis after waste heat boiler recycles heat
The regenerated flue gas of cracking.
Preferably, the regenerated flue gas of the catalytic cracking, after waste heat boiler recycles heat, from the spray drying tower
Bottom or top or top and bottom flow into the spray drying tower.
Preferably, average grain diameter < 100 micron after the concentrating spent liquor atomization；Leave the regeneration of the spray drying tower
Flue-gas temperature normal temperature > 100 DEG C, it is minimum to be not less than 80 DEG C；The total solids content for leaving dust removal installation is less than 20mg/Nm3。
Compared with prior art, the processing of a kind of catalytic cracking unit desulfurization wastewater of the utility model and flue gas thermal coupling fills
It sets by combining two kinds of techniques of multiple-effect evaporation and spray drying, realizes the purpose to the processing of catalytic cracking unit desulfurization wastewater.
Detailed description of the invention
Fig. 1 is the system tray of the processing unit of a kind of catalytic cracking unit desulfurization wastewater of the utility model and flue gas thermal coupling
Structure schematic diagram；
Fig. 2 is the structural schematic diagram of pre-concentration unit 1 in the utility model specific embodiment；
Fig. 3 is the structural schematic diagram that unit 2 is spray-dried in the utility model specific embodiment.
Specific embodiment
Below by way of specific specific example and the embodiments of the present invention is described with reference to the drawings, those skilled in the art
Member can be understood easily the further advantage and effect of the utility model by content disclosed in the present specification.The utility model also may be used
It is implemented or is applied by other different specific examples, the various details in this specification can also be based on different viewpoints and answer
With, carried out under the spirit without departing substantially from the utility model it is various modification and change.
Fig. 1 is the system tray of the processing unit of a kind of catalytic cracking unit desulfurization wastewater of the utility model and flue gas thermal coupling
Structure schematic diagram.As shown in Figure 1, a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling of the utility model,
Include:
Pre-concentration unit 1, for carrying out multiple-effect evaporation pre-concentration to catalytic cracking unit (FCC) desulfurization wastewater, so that dense
The Na of concentrate after contracting2SO4Mass concentration is 20-40%, and temperature is 60-80 DEG C.
Specifically, as shown in Fig. 2, pre-concentration unit 1 includes Multi-effect evaporator system 100, pumped vacuum systems 101, condensation
System 102 and concentrate remove spraying system 103, wherein Multi-effect evaporator system 100, for the FCC desulfurization wastewater to feeding
Multiple-effect evaporation is carried out, the medium of multiple-effect evaporation can use steam, can also be using the condensed water in high temperature or low temperature in device
Position hot water, pumped vacuum systems 101 connect Multi-effect evaporator system 100, for reducing multi-effect evaporator system by vacuum system
The operating pressure of evaporator, makes it below normal pressure, to reduce the operation temperature of evaporator in system 100；Condenser system 102, is used for
Cooling recycling is carried out to the steam water outlet of every level-one multiple-effect evaporation of Multi-effect evaporator system 100, the water of recycling can be used as and urge
The technique supplement for changing flue gas desulfurization uses water；Concentrate removes spraying system 103, for 100 multiple-effect evaporation of Multi-effect evaporator system
Concentrate after pre-concentration carries out spraying treatment, and concentrate is sent into spray drying unit 2 by treated.
In the utility model, the waste liquid that regeneration fume from catalytic cracking desulphurization system is discharged is arranged with power plant wet desulphurization
The waste liquid put is different, is mainly manifested in contained salts substances difference, and chloride ion content is different in waste water.Generally, power plant is wet
Method desulfurization, the salt main component in waste water are chloride, such as sodium chloride, magnesium chloride, calcium chloride, and the chlorine in water is abolished in discharge
Ion concentration is normally close to 20000mg/L, and the waste liquid that regeneration fume from catalytic cracking desulfurization is discharged, main component Na2SO4,
Chloride ion content in waste water is generally less than 1000Mg/L.
In addition, the waste liquid that regeneration fume from catalytic cracking desulphurization system is discharged, the waste liquid that is discharged with power plant wet desulphurization
PH value it is also different, the waste water of general power plant smoke desulfurization by wet method direct emission, pH value is generally in 6.5-7 or so, slant acidity, and
The waste water that catalytic cracked regenerated desulfurization is discharged, pH value is most of in 7-7.5 in 6-9, neutral meta-alkalescence, so, catalytic cracking
The desulfurization wastewater of device regenerated flue gas is significantly less than the waste water that calcium carbide wet desulphurization is arranged for corrosivity.
Therefore, regeneration fume from catalytic cracking desulfurization wastewater, because the chloride ion content of system is not high, contained salt industry is mainly
Na2SO4, solubility is high, as long as the content of solute is lower than 40g/100ml, at 30 DEG C or more, Na in waste water2SO4The product of class
It will not be folded in evaporation equipment.
In the utility model specific embodiment, the utility model is by the Na in catalytic desulfurization waste water2SO4Mass concentration
By multiple-effect evaporation technology, 20w% is increased to 40%, wherein multiple-effect evaporation can be economic benefits and social benefits, triple effect or quadruple effect, can be flexible
Selection, the selection of evaporator quantity is mainly determined according to the available place situation in scene, for example, can adopt in place anxiety
With double-effect evaporation, in grassroot project or more relaxed place, using four-effect evaporation, the medium of multiple-effect evaporation can be using steaming
Vapour, can also be using the condensed water in high temperature or low temperature position hot water in device, wherein using steam as the heat source heated, generally
Using triple effect or quadruple effect, using hot water (condensed water) as heat source, using economic benefits and social benefits or triple effect.
In the utility model specific embodiment, Multi-effect evaporator system 100 is mating to use pumped vacuum systems, it is therefore an objective to logical
Pumped vacuum systems is crossed, the operating pressure of Multi-effect evaporator system is reduced, makes it below normal pressure, to reduce the operation temperature of evaporator
The operation temperature of degree, general afterbody evaporator is controlled at 60-80 DEG C.
In the utility model specific embodiment, the water outlet of steam at the top of every level-one multiple-effect evaporation, by condenser system (
Cooler can be used in the utility model specific embodiment) cooling recycling is carried out, the water of recycling can be used as catalysis flue gas desulfurization
Technique supplement use water.
In the utility model specific embodiment, the recycle-water that multi-effect evaporation system steams typically constitutes from total wastewater feed
The main technique norm controlling of 60-80%, pre-concentration unit 1 are as follows:
60-80 DEG C of temperature of afterbody evaporator operation；
Waste liquid Na after concentration2SO4Mass concentration 20-40%；
Concentrate chlorine ions concentration: < 3000mg/L.
In the present invention, due to the total amount of the regenerated flue gas of catalytic cracking be it is little, generally in 100000-
400000Nm3/ h, the normal temperature for leaving waste heat boiler is 160-220 DEG C, so being down to 100 DEG C from 160 DEG C can evaporate
Water has a maximum value for every covering device.If without pre-concentration, it is impossible to will be produced by catalysis flue gas desulfurization
All waste water be all evaporated with the flue gas heat in device,
It is spray-dried unit 2, for crystallization to be dried using flue gas to the concentrate after multiple-effect evaporation pre-concentration.
Specifically, as shown in figure 3, spray drying unit 2 further comprises:
Spray drying tower 20, spray drying tower 20 include drying tower tower body 200 and atomization system 201, wherein after concentration
Desulfurization waste liquor is atomized concentrating spent liquor by atomization system 201, concentrating spent liquor is atomized with spray drying tower 20 is pumped into
At microlayer model, in the utility model specific embodiment, atomization system 201 is set to the top of spray drying tower, after atomization
Particle sprays at the top of drying tower, and the moisture content in microlayer model is evaporated rapidly using the flue gas in spray drying tower, and crystallization is precipitated, knot
Brilliant salt particle small part settles in drying tower 20, is discharged by bottom, most of to be carried by flue gas, leaves drying tower 20, into
Enter dust removing units 21, in the utility model specific embodiment, in spray drying tower for spray drying flue gas using
The regenerated flue gas of catalytic cracking after waste heat boiler recycles heat, can be from the bottom of drying tower 20 or from top, bottom
Into drying tower 20, that is to say, that the regenerated flue gas of catalytic cracking, through waste heat boiler recycle heat after, from bottom or from top,
Bottom flows into spray drying tower 20, and the moisture content in microlayer model is reproduced flue gas and evaporates rapidly, and crystallization is precipitated, and crystal salt particle lacks portion
Divide and settled in drying tower 20, is discharged by bottom, it is most of to be carried by flue gas, drying tower 20 is left, into dust removing units 21.
Dust removing units 21 will be contained in regenerated flue gas for being dusted processing to the regenerated flue gas for leaving drying tower
Catalyst dust is filtered and is recycled together with the salt of crystallization, and the regenerated flue gas after dedusting then enters the suction of wet desulphurization
Receive tower.In the utility model specific embodiment, filtering material used by dust removing units 21 can be organic polymer,
It can be the porous material of inorganic material firing, the utility model is not limited.
As it can be seen that the utility model spray drying enters the regenerated flue gas before wet desulfuration tower after using remaining pot, i.e., to device
Remaining pot heat recovery without influence, after the spray-dried tower of regenerated flue gas, evaporated the moisture in concentrate, temperature reduces,
After entering the absorption tower of wet desulphurization in this way, the water of absorption tower evaporation will be reduced, and the heat of regenerated flue gas first gives desulfurization dense
Contracting liquid is dry, reduces flue gas into the temperature on absorption tower, reduces the evaporated water on absorption tower.The utility model uses dress
The coupling manner of the heat of interior regenerated flue gas is set, in addition supplement water of the recycle-water of multiple-effect evaporation as desulfurizing tower, the idol of heat
Conjunction mode, greatly reduces total amount of makeup water of desulphurization system, and reduced process water consumption is substantially equal to absorption tower discharge waste liquid
Contained in total Water.I.e. using all moisture in waste liquid that after the utility model, desulfurizing tower is discharged, all it is utilized,
I.e. the utility model can all recycle all moisture in the waste liquid of absorption tower, moreover, the regeneration cigarette of the utility model
Gas has been subjected to dust removal process into before wet desulfuration tower, so it has been substantially free of catalyst into the flue gas of wet desulfuration tower,
To substantially reduce the abrasion of absorption system.
In the utility model specific embodiment, concentrate after multiple-effect evaporation pre-concentration, solute concentration is improved to 20-
40w%, can be admitted to spray drying unit 2 and crystallization operation is dried by 60-80 DEG C of temperature.
Being spray-dried unit includes spray drying tower and dust removing units, and spray drying tower then includes drying tower tower body and atomization
High speed atomisation wheel or high-efficiency atomizing nozzle can be used in system, atomization system, in the utility model specific embodiment, after concentration
Desulfurization waste liquor with the top of spray drying tower is pumped into, mist is carried out to concentrating spent liquor with high speed atomisation wheel or high-efficiency atomizing nozzle
Change.
The regenerated flue gas of catalytic cracking flows into spray drying tower then after waste heat boiler recycles heat, in drying tower,
Particle after atomization sprays at the top of drying tower, and regenerated flue gas enters drying tower from the bottom of drying tower or from top, bottom,
In drying tower, concentrating spent liquor is atomized into microlayer model, and the moisture content in microlayer model is reproduced flue gas and evaporates rapidly, and crystallization is precipitated, knot
Brilliant salt particle small part settles in drying tower, is discharged by bottom, most of to be carried by flue gas, leaves drying tower, into removing
Dirt unit.
The regenerated flue gas for leaving drying tower will be urged into the dust removal by filtration device of dust removing units contained in regenerated flue gas
Agent dust is filtered and is recycled together with the salt of crystallization.
In the utility model specific embodiment, it is spray-dried the main control parameters of unit 2:
Into the regenerated flue gas flow and temperature of spray drying tower: the normal exhaust gas temperature of waste heat boiler, most of device
For operation temperature at 160-220 DEG C, regenerated flue gas amount can be the regenerated flue gas of part, can also be whole regenerated flue gas；
Average grain diameter after Waste liquid atomization: < 100 microns；
Regenerated flue gas temperature normal temperature > 100 DEG C of spray drying tower are left, it is minimum to be not less than 80 DEG C；
Leave total solids content: less than 20mg/Nm of dust removal installation3。
All salts caused by regeneration flue gas desulfurization are removed system by the utility model in solid form, thus greatly
The big influence reduced to water environment, reduces the impact to enterprise's sewage disposal system or urban sewage treatment system.
It should be noted that the processing catalytic cracking flue gas that the utility model is combined using multiple-effect evaporation with spray drying
Desulfurization outlet Na2SO4Technique, being not limited to multiple-effect evaporation is economic benefits and social benefits, triple effect or quadruple effect, and being also not necessarily limited to spray drying is using machine
Tool atomization or the atomised form using two-fluid spray nozzle, the intake type for being not limited to drying tower is top air inlet or top, bottom
Air inlet simultaneously is also not necessarily limited to cleaner using what material, what form.
In conclusion a kind of catalytic cracking unit desulfurization wastewater of the utility model and the processing unit of flue gas thermal coupling pass through
In conjunction with two kinds of techniques of multiple-effect evaporation and spray drying, the purpose to the processing of catalytic cracking unit desulfurization wastewater is realized.
Compared with prior art, the utility model has the advantages that
1, energy consumption is few: the energy of the utility model is used primarily on multiple-effect evaporation, if using hot water as heat source,
Energy consumption will further decrease, and spray drying tower atomizer and pumped vacuum systems need to consume a small amount of electric power, but compare vaporation-type
It is dry, low energy consumption.
2, invest low: the pre-concentration that the utility model uses, control chloride ion content are less than 3000mg/L, solute concentration
20-40%, so, the component (pump, evaporator, heat exchanger, instrument etc.) contacted with liquid can use low nickel alloy or two-phase
The inexpensive materials such as stainless steel are not needed using expensive Langaloy or titanium alloy material, the normal operating pressure of spray drying tower
Power is 3000-5000pa, and 160-220 DEG C of gas inlet temperature, for flue gas exit temperature greater than 110 DEG C, drying tower can use carbon
Steel or carbon steel lining anticorrosive material mode, invest it is lower, cleaner can use polymer material, shell can be used carbon steel or
Carbon steel serves as a contrast resistant material, and the construction investment of project is low, and maintenance cost is relatively low.
3, reduce the water consume of catalytic cracking unit: wet desulphurization device needs discharge part waste water, using the utility model
Afterwards, all moisture in the waste liquid of the part outlet, are all utilized, so, using the utility model, catalysis will be reduced and split
The consumption of water is set in makeup, and reduced water is equal to water contained in the desulfurization waste liquor of discharge.
4, the impact to sewage farm is reduced, saline sewage is handled with the utility model, high saline sewage pair will be eliminated
There is impact in sewage farm.
5, the abrasion of desulphurization system is reduced.The catalyst of catalytic cracking has very strong abrasion energy to pump, absorption tower body
Power, after the cleaner removal of the utility model, by the abrasion for the system that substantially reduces.
The above embodiments are only illustrative of the principle and efficacy of the utility model, and not for limitation, this is practical new
Type.Anyone skilled in the art can repair above-described embodiment under the spirit and scope without prejudice to the utility model
Decorations and change.Therefore, the rights protection scope of the utility model, should be as listed in the claims.
Claims (10)
1. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling, comprising:
Pre-concentration unit, for carrying out the processing of multiple-effect evaporation pre-concentration to catalytic cracking unit desulfurization wastewater so that dense after concentration
The Na of contracting liquid2SO4Mass concentration is 20-40%, and temperature is 60-80 DEG C, and the concentrate after concentration is sent into spray drying list
Member；
It is spray-dried unit, crystallization is dried using flue gas to the concentrate after multiple-effect evaporation pre-concentration.
2. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as described in claim 1, feature
It is, the pre-concentration unit includes:
Multi-effect evaporator system carries out multiple-effect evaporation to the catalytic cracking unit desulfurization wastewater of feeding；
Pumped vacuum systems connects the Multi-effect evaporator system, to reduce the Multi-effect evaporator system by pumped vacuum systems
The operating pressure of middle evaporator reduces the operation temperature of evaporator；
Condenser system connects the Multi-effect evaporator system, with every level-one multiple-effect evaporation to the Multi-effect evaporator system
Steam water outlet carries out cooling recycling；
Concentrate removes spraying system, connects the Multi-effect evaporator system, with pre- to the Multi-effect evaporator system multiple-effect evaporation
Concentrate after concentration carries out spraying treatment, and concentrate is sent into spray drying unit by treated.
3. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 2, feature
It is, the multiple-effect evaporation medium of the Multi-effect evaporator system, using the condensed water in high temperature or low temperature position heat in steam or device
Water.
4. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 2, feature
Be: the operation temperature of the afterbody evaporator of the Multi-effect evaporator system is controlled at 60-80 DEG C.
5. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 2, feature
It is: chlorine ions concentration < 3000mg/L of the concentrate after pre-concentration unit multiple-effect evaporation concentration.
6. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as described in claim 1, feature
It is, the spray drying unit includes:
Spray drying tower, the spray drying tower include drying tower tower body and atomization system, and the desulfurization waste liquor after concentration is sent into
After the spray drying tower, concentrating spent liquor is atomized by the atomization system, concentrating spent liquor is atomized into microlayer model, it is micro-
Using the smoke evaporative in spray drying tower, crystallization is precipitated moisture content in drop, and crystal salt particle small part is described spraying dry
Sedimentation, is discharged by bottom in dry tower, most of to be carried by flue gas, is left the spray drying tower and is entered dust removing units；
Dust removing units, for being dusted processing to the flue gas for leaving drying tower, by catalyst dust contained in flue gas and knot
Brilliant salt is filtered together and is recycled, and the flue gas after dedusting is sent into the absorption tower of wet desulphurization.
7. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 6, feature
Be: the atomization system is set to the top of the spray drying tower, by the particle after atomization from the spray drying tower top
Portion sprays into.
8. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 6, feature
Be: the flue gas in the spray drying tower for spray drying is the regeneration of the catalytic cracking after waste heat boiler recycles heat
Flue gas.
9. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 8, feature
It is: the regenerated flue gas of the catalytic cracking, after waste heat boiler recycles heat, from the bottom or top of the spray drying tower
Or top and bottom flow into the spray drying tower.
10. a kind of processing unit of catalytic cracking unit desulfurization wastewater and flue gas thermal coupling as claimed in claim 8, feature
It is: average grain diameter < 100 micron after the concentrating spent liquor atomization；Leave the regenerated flue gas temperature of the spray drying tower just
Normal temperature > 100 DEG C, it is minimum to be not less than 80 DEG C；The total solids content for leaving dust removal installation is less than 20mg/Nm3。
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