CN201192639Y - Catalyst coke burning regeneration apparatus for straight-run gasoline non-hydrogenation upgrading process - Google Patents
Catalyst coke burning regeneration apparatus for straight-run gasoline non-hydrogenation upgrading process Download PDFInfo
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- CN201192639Y CN201192639Y CNU200820074042XU CN200820074042U CN201192639Y CN 201192639 Y CN201192639 Y CN 201192639Y CN U200820074042X U CNU200820074042X U CN U200820074042XU CN 200820074042 U CN200820074042 U CN 200820074042U CN 201192639 Y CN201192639 Y CN 201192639Y
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Abstract
The utility model relates to a coke-burning device for regenerating the non-hydrogenation upgrading catalyst for straight-run gasoline. A non-purified air dewatering tank (D-113) is disposed on an outlet pipeline of a heat exchanger (E-102) and connected with an air inlet coke-burning pipeline. A pipeline led from the original non-purified air main pipeline at one end thereof is connected with the middle part of the non-purified air dewatering tank (D-113), and a pipeline led from the top of the non-purified air dewatering tank (D-113) is connected with the outlet pipeline the shell side of the heat exchanger (E-102). Under the control of a feeding control valve on the lower section C4 of a reactor (R-101), non-purified air enters the reactor (R-101). The coke-burning device has the advantages that the coke-burning time in the sixth period is 5 days shorter than the last period; 55,000 kW h power, about 31,000 tons of recycled water, a large amount of fuel gas and nitrogen are saved; the process loads of naphtha and the C4 fraction are respectively increased by 648 tons and 660 tons based on the refining loads of the naphtha of 5.4t/h and the C4 fraction of 5.5t/h; and the yields of the clean component oil and the vehicle liquefied gas are respectively improved by 745 tons and about 565 tons.
Description
Technical field
The utility model relates to the catalyst regeneration technical field, particularly relates to a kind of device of charring straight-run gasoline gasoline upgrading catalyst regeneration.
Background technology
The direct steaming gasoline non-hydrogen modification technology of Research Institute of Petro-Chemical Engineering exploitation is as raw material with a certain proportion of direct steaming gasoline and surplus carbon four, superimposed and a series of complex reactions such as dehydrocyclization, direct steaming gasoline selective splitting, isomery, oligomerisation and dehydrocyclization reach the purpose that improves octane number of direct distillation gasoline through C 4 olefin.This technology can be the low high-knock rating gasoline blend component of olefin(e) centent with low-octane direct steaming gasoline and carbon four feedstock conversion, be used to be in harmonious proportion catalytically cracked gasoline, reduce the olefin(e) centent of blended gasoline, blended gasoline is up to state standards, also can produces the blend component of motor liquified gas simultaneously.Because the characteristics of gasoline non-hydrogen upgrading reaction, cause on the catalyst carbon distribution very fast, the inside reactor catalysqt deactivation just need carry out coke burning regeneration, so that catalyst regains the production that activity is carried out next cycle, the cycle of operation of single reactor is greatly about about one month, and the employing intermittently operated, the mode of production of the regeneration of stopping work just will certainly produce tremendous influence because of long energy consumption and economic benefit to device of the time of burning.
Existing regeneration is burnt device as shown in Figure 1,1) equipment connects and operating process is after regeneration cycle compressor (K-102) exit gas burns jar (D-102) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side to heat exchanger (E-101) tube side to air cooler (A-101) cooler (E-104) shell side to heat exchanger (E-103) shell side to heating furnace (F-101) reactor (R-101) through heat exchanger (E-101) shell side, returns regeneration cycle compressor (K-102) and enter the mouth and circulate.2) reactor (R-101) from top to bottom catalyst be divided into three sections, bed is detail as per following table:
Reactor (R-101) beds distribution table
| First section of reactor (epimere) | Second section of reactor (stage casing) | The 3rd section of reactor (hypomere) |
| The epimere ground floor | The stage casing ground floor | The hypomere ground floor |
| The epimere second layer | The stage casing second layer | The hypomere second layer |
| The 3rd layer of epimere | The 3rd layer in stage casing | The 3rd layer of hypomere |
Regeneration is burnt method of operating and is:
Catalyst in reactor is through after the operation of some cycles, and its loss of activity can be according to its performance situation, the renovation process that burns in the collector and its activity is restored.
1. when the temperature in the reactor that cuts out (R-101) is reduced to 230～250 ℃, with blind plate with pipeline before reactor (R-101) the feedstock oil inlet, the pipeline that reactor (R-101) is exported to heat exchanger (E-101) cuts off fully, take the blind plate of reactor (R-101) to regenerative system apart, reactor this moment (R-101) is communicated with regenerative system.
2. open regeneration cycle compressor (K-102), slowly charge into nitrogen to regeneration cycle compressor (K-102) porch, regeneration cycle compressor (K-102) exit gas through heat exchanger (E-101) shell side to heat exchanger (E-103) shell side to heating furnace (F-101) enter reactor (R-101) enter to cooler (E-104) shell side to heat exchanger (E-101) tube side to air cooler (A-101) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side burn jar (D-102) after, return regeneration cycle compressor (K-102) and circulate, until burning jar (D-a 102) pressure to 0.15～0.3Mpag; Regulate regeneration cycle compressor (K-102) and be exported to the pipeline valve (manual bypass) that burns jar (D-102), require down so that the outlet pressure of regeneration cycle compressor (K-102) satisfies equipment, the systemic circulation amount is carried gradually to maximum (regeneration cycle compressor K-102 design load 10000～12200Nm
3/ h).
3. with the reactive moieties nitrogen replacement, go out the interior feedstock oil of reactor (R-101) by burning jar (D-102) jar undercutting simultaneously.Must guarantee that system's nitrogen replacement is qualified, not contain feedstock oil.
4.F-101 begin heating; And carry out (table 3) according to the catalyst regeneration condition of burning.
The catalyst in-situ regeneration burns condition
| Operating procedure | Temperature, ℃ | Operating time, h | Heating rate, ℃/h | Oxygen content, v% | The operation medium |
| Heat up | Normal temperature～400 | 8 | 25 | 0 | High nitrogen |
| Constant temperature burns | 400 | 120 | 0.5 | High nitrogen+air | |
| Constant temperature burns | 400 | 0.5~21 | High nitrogen+air | ||
| Heat up | 400～450 | 2 | 25 | 21 | Air |
| Constant temperature burns | 450 | 21 | Air | ||
| Cooling | 450～250 | 6 | 33 | 21 | Air |
In the burning process as required, mend into air to regeneration cycle compressor (K-102) porch, burn O in jar (D-102) tank deck control valve control system pressure and the circulating air by adjusting simultaneously
2Concentration.
6. according to reactor bed temperature rise situation, progressively go into amount and improve the temperature of burning in the reactor by improving the benefit that purifies wind; Guarantee 50～60 ℃ of bed temperature rises (temperature difference in the reactor between each section ground floor and the 3rd layer), maximum temperature is lower than 450 ℃ in the reactor; If sulfur content is higher in the catalyst carbon deposit, then need to mend alkali lye to burning (D-102), to reduce the sulfide content in the recyclegas by interim pipeline.
7. reach 440～450 ℃ when feeding a large amount of air and burning temperature, and bed there has not been obvious temperature rise, then burns end, stops bubbling air.
8. reduce heating furnace (F-101) outlet temperature gradually, make reactor batch temperature reduce to 280～300 ℃, cooling rate＜50 ℃/h.
9. stop heating furnace (F-101) heating, stop regeneration cycle compressor (K-102).
Slowly with system gas emptying to normal pressure or depend on the circumstances.Take the pressure release purging method to check in heat exchanger (E-101, E-103, E-102), heating furnace (F-101), air cooler (A-101), the cooler (E-104) whether accumulate foreign material, if any, can take to fill the compression air and purge (should notice during purging that the vent gas incident of hurting sb.'s feelings takes place), waste water, the refuse that will burn at last in jar (D-102) are discharged, and purge clean.
Replace 11. charge into nitrogen, qualified after, as reactor batch temperature＜250 ℃, blind plate is closed in removable commutation, reactor is standby.
I go into operation on June 25th, 2006 by company's non-hydrogen modifying apparatus, find that through the operation in four cycles regeneration burns fate the pernicious phenomenon that increases progressively is gradually arranged, existing with above-mentioned situation and go into operation and burn in electric equipment ruuning situation sum up and be listed as follows:
1, burns the time
| Burn the cycle | From date | Date of expiry | The regeneration fate |
| First | 06.08.23. | 06.09.05. | 13 |
| Second | 06.10.24. | 06.11.06. | 14 |
| The 3rd | 06.12.27. | 07.01.12. | 15 |
| The 4th | 07.02.26. | 07.03.15. | 16 |
2, go into operation and the electric equipment power consumption situation contrast table (is example with the period 4) when burning
Summary of the invention
Because surplus carbon four devices of our factory adopt the batch production of three-section fixed-bed reactor at first, so by last table as can be known: every prolongation one day is burnt in regeneration, device just is equivalent to stopped work one day more, energy consumption and many one day economic losses of will fecund giving birth to one day, for this reason, in order to solve the deficiencies in the prior art, leader and technical staff adopt kinds of experiments, research, reform, innovation, carbon four advances reactor line in the use device, designs during the period 5, regeneration was burnt, transforms and finish.With the original reactor single channel air intake of setting out on a journey, be transformed into set out on a journey and following road two-way simultaneously air intake burn.Regeneration has obtained sufficient proof in burning in the period 5 for the reasonability of transformation project and validity.
Concrete device of the present utility model is as follows:
The device of charring straight-run gasoline gasoline upgrading catalyst regeneration of the present utility model, comprise reactor (R-101), heating furnace (F-101), heat exchanger, air cooler (A-101), cooler (E-104), gas compressor with reciprocating (K-102), burn jar (D-102), non-purification wind drain sump (D-113), control valve and reactor (R-101), direct steaming gasoline non-hydrogen modifying apparatus reactive moieties regeneration gas compressor (K-102) suction line is provided with an air intake and burns pipeline, one end of pipeline is arranged on the suction line of regeneration gas compressor (K-102), and the other end links to each other with purification wind house steward; Wherein heat exchanger (E-102) outlet line is provided with non-purification wind drain sump (D-113), burning pipeline with air intake is connected, pipeline one end is drawn a pipeline and is linked to each other with the middle part of non-purification wind drain sump (D-113) from installing the total pipeline of original non-purification wind, draw a pipeline links to each other with heat exchanger (E-102) shell side outlet line from the top of non-purification wind drain sump (D-113), under the control of the hypomere C4 charging control valve of reactor (R-101), non-purification wind enters reactor (R-101).
The method of operating of the device of charring straight-run gasoline gasoline upgrading catalyst regeneration of the present utility model, be that non-purification wind burns pipeline through air intake after non-purification wind drain sump (D-113) dehydration, the hypomere C4 charging control valve of autoreactor (R-101) enters reactor (R-101) hypomere, come out to enter heat exchanger (E-103) tube side from reactor (R-101) bottom, remove heat exchanger (E-102) tube side then, to heat exchanger (E-101) tube side, enter air cooler (A-101), enter cooler (E-104) shell side again, enter to burn and return K-102 inlet after jar (D-102) and circulate.
The method of operating of the device of described charring straight-run gasoline gasoline upgrading catalyst regeneration is: when the temperature in the reactor is reduced to 250 ℃～280 ℃, with blind plate feedstock oil is entered the mouth to the preceding pipeline of heat exchanger (E-101) and to cut off fully, take the blind plate of reactor to regenerative system apart, this moment, reactor was communicated with regenerative system; Two or three sections C4 feeding lines that will burn jar (D-102) and absorbing-stabilizing system and reactor separate with blind plate; Blind plate 5 this part pipeline nitrogen replacement with reactive moieties and E-102 shell side outlet line to hypomere control valve 4 to reactor, go out the interior feedstock oil of reactor by burning jar (D-102) jar undercutting simultaneously, mend into air to regeneration cycle compressor (K-102) porch and reactor hypomere bed, high some temperature is at 450 ℃～470 ℃; Reach 440～450 ℃ when feeding a large amount of air and burning temperature, constant temperature stopped bubbling air after 4 ~ 5 hours, adopted N2 to replace O to the reactor
2Content then burnt end less than 0.5% o'clock.
The method of operating of the device of charring straight-run gasoline gasoline upgrading catalyst regeneration of the present utility model, adopt the method for two-way air intake, the first via be regeneration cycle compressor (K-102) exit gas through heat exchanger (E-101) shell side to heat exchanger (E-103) shell side to heating furnace (F-101) to reactor (R-101) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side to heat exchanger (E-101) tube side to air cooler (A-101) to cooler (E-104) shell side after burn jar (D-102), returning regeneration cycle compressor (K-102) inlet circulates.The second the tunnel: being an end draws the pipeline of a Φ 32 * 2.5 and links to each other with newly-increased middle part of burning special-purpose non-purification wind jar (D-113) from installing the total pipeline of original non-purification wind (Φ 89 * 4), draw a pipeline (Φ 47 * 3.5) and heat exchanger (E-102) shell side outlet line (illustrate: E-102 shell side outlet line just uses when ordinary production before the utility model from newly-increased top of burning special-purpose non-purification wind jar (D-113), the utility model has utilized blind plate 5 this part pipeline to reactor hypomere control valve 4 to reactor of this pipeline to enter the passage of reactor as non-purification wind) link to each other, under the control of the hypomere control valve of reactor (R-101), non-purification wind enters reactor (R-101), come out to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side to heat exchanger (E-101) tube side to air cooler (A-101) in the bottom of reactor (R-101) to cooler (E-104) shell side after burn jar (D-102), returning regeneration cycle compressor (K-102) inlet circulates.
Concrete steps are as follows:
1) when the temperature in the reactor is reduced to 250 ℃～280 ℃, with blind plate feedstock oil is entered the mouth to the preceding pipeline of heat exchanger (E-101) and to cut off fully, take the blind plate of reactor apart to regenerative system, this moment, reactor was communicated with regenerative system; Two or three sections C4 feeding lines that will burn jar (D-102) and absorbing-stabilizing system and reactor separate with blind plate.
2) open regeneration cycle compressor (K-102), slowly charge into nitrogen to regeneration cycle compressor (K-102) porch, regeneration cycle compressor (K-102) exit gas through heat exchanger (E-101) shell side to heat exchanger (E-103) shell side to heating furnace (F-101) enter reactor (R-101) enter to cooler (E-104) shell side to heat exchanger (E-101) tube side to air cooler (A-101) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side burn jar (D-102) after, return regeneration cycle compressor (K-102) and circulate, until burning jar (D-a 102) pressure to 0.15～0.3Mpag; Regulate regeneration cycle compressor (K-102) and be exported to the pipeline valve (manual bypass) that burns jar (D-102), require down so that the outlet pressure of regeneration cycle compressor (K-102) satisfies equipment, the systemic circulation amount is carried gradually to maximum (regeneration cycle compressor K-102 design load 10000～12200Nm
3/ h).
3) with blind plate 5 this part pipeline nitrogen replacement of reactive moieties and E-102 shell side outlet line, go out the interior feedstock oil of reactor by burning jar (D-102) jar undercutting simultaneously to hypomere control valve 4 to reactor.Must guarantee that system's nitrogen replacement is qualified, not contain feedstock oil.
4) heating furnace (F-101) begins heating; And burn condition (following table) according to catalyst regeneration and carry out.
The catalyst in-situ regeneration burns condition
| Operating procedure | Temperature, ℃ | Operating time, h | Heating rate, ℃/h | Oxygen content, v% | The operation medium |
| Heat up | Normal temperature～400 | 8 | 25 | 0 | High nitrogen |
| Constant temperature burns | 400 | 120 | 0.5 | High nitrogen+air | |
| Constant temperature burns | 400 | 0.5~21 | High nitrogen+air | ||
| Heat up | 400～450 | 2 | 25 | 21 | Air |
| Constant temperature burns | 450 | 21 | Air | ||
| Cooling | 450～250 | 6 | 33 | 21 | Air |
5) in the burning process as required, mend into air and regulate its flow of control to regeneration cycle compressor (K-102) porch and reactor hypomere bed, be strictly on guard against temperature rise too fast or too high (high some temperature is controlled at 450 ℃～470 ℃, definitely can not above 470 ℃); Burn jar (D-102) tank deck by adjusting simultaneously and burn O in emptying control valve control system pressure and the circulating air
2Concentration.
6), progressively go into amount and improve the temperature of underpaying in the reactor by the benefit that improve to purify wind and non-purification wind according to reactor bed temperature rise situation; Guarantee 50～60 ℃ of bed temperature rises (temperature difference in the reactor between each section ground floor and the 3rd layer), maximum temperature is lower than 470 ℃ in the reactor; If sulfur content is higher in the catalyst carbon deposit, then need to mend alkali lye to burning (D-102), to reduce the sulfide content in the circulating air by interim pipeline.
7) reach 440～450 ℃ (the peak temperature stage of reaction in) when feeding a large amount of air and burning temperature, and bed has not had obvious temperature rise, constant temperature stops bubbling air after four to five hours, and employing N2 replaces O to the reactor
2Content then burnt end less than 0.5% o'clock.
8) reduce heating furnace (F-101) outlet temperature gradually, make reactor batch temperature reduce to 240 ℃～250 ℃, cooling rate＜50 ℃/h.
9) after qualified, change relevant blind plate, off-response device terminal valve is opened the by-pass valve, and reactor is standby
Owing to increased line equipment, the utility model unlike the prior art be:
Two or three sections C4 feeding lines with reactor (R-101) in the step 1 separate with blind plate, are to cause the violent temperature of burning in the reactor, pressure superelevation reactor (R-101) to be leaked and the damage catalyst in order to prevent in the air because of the tight C4 raw material of valve closing bleeds to burn.
In the step 5 in the burning process as required, mend into air and regulate its flow of control to K-102 porch and the 3rd section bed of reactor, be in order to make catalyst wherein carbon deposit and burnt matter of burn off under steady, safe condition; If temperature rise too fast or too high (high some temperature is above 470 ℃) will exceed catalyst safe handling scope, cause catalyst breakage.
What change in the step 7 is according to reactor bed temperature rise situation, progressively improves the benefit of burning temperature and air and goes into amount; Guarantee 50 ~ 60 ℃ of bed temperature rises, maximum temperature is lower than 470 ℃ in the device, is in order to make catalyst burn as soon as possible burn off wherein carbon deposit and burnt matter under steady, safe condition.
Description of drawings
Fig. 1: the process chart of prior art;
Fig. 2: process chart of the present utility model.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is elaborated:
Present embodiment adopts device and the flow process of Fig. 2, the device of charring straight-run gasoline gasoline upgrading catalyst regeneration of the present utility model comprises 1 of reactor (R-101), 1 in heating furnace (F-101), 3 groups on heat exchanger (E-101/1.2, E-102/1.2, E-103), 1 of air cooler (A-101), cooler E-104) 1 group, 1 of gas compressor with reciprocating (K-102), burn 4 of jar (D-102) 1,1 of a non-purification wind drain sump (D-113), control valves (burn air intake, burn emptying, D-102 cuts water, C4 removes down section feeding).The method of operating of the device of charring straight-run gasoline gasoline upgrading catalyst regeneration of the present utility model, adopt the method for two-way air intake, the first via be regeneration cycle compressor (K-102) exit gas through heat exchanger (E-101) shell side to heat exchanger (E-1030 shell side to heating furnace (F-101) to reactor (R-101) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side to heat exchanger (E-101) tube side to air cooler (A-101) to cooler (E-104) shell side after burn jar (D-102), returning regeneration cycle compressor (K-102) inlet circulates.The second the tunnel: being an end draws the pipeline of a Φ 32 * 2.5 and links to each other with the middle part of newly-increased non-purification wind drain sump (D-113) from installing the total pipeline of original non-purification wind (Φ 89 * 4), drawing a pipeline (Φ 47 * 3.5) from the top of newly-increased non-purification wind drain sump (D-113) links to each other with heat exchanger (E-102) shell side outlet line, under the control of the hypomere control valve of reactor (R-101), non-purification wind enters reactor (R-101).
E-102 shell side outlet line just uses when ordinary production before the utility model, and the utility model has utilized blind plate 5 this part pipeline to hypomere control valve 4 to reactor of this pipeline to enter the passage of reactor as non-purification wind.
Concrete steps are as follows:
1). when the temperature in the reactor is reduced to 250 ℃～280 ℃, with blind plate feedstock oil is entered the mouth to the preceding pipeline of heat exchanger (E-101) and to cut off fully, take the blind plate of reactor to regenerative system apart, this moment, reactor was communicated with regenerative system; Two or three sections C4 feeding lines that will burn jar (D-102) and absorbing-stabilizing system and reactor separate with blind plate.
2). open regeneration cycle compressor (K-102), slowly charge into nitrogen to regeneration cycle compressor (K-102) porch, regeneration cycle compressor (K-102) exit gas through heat exchanger (E-101) shell side to heat exchanger (E-103) shell side to heating furnace (F-101) enter reactor (R-101) enter to cooler (E-104) shell side to heat exchanger (E-101) tube side to air cooler (A-101) to heat exchanger (E-103) tube side to heat exchanger (E-102) tube side burn jar (D-102) after, return regeneration cycle compressor (K-102) and circulate, until burning jar (D-a 102) pressure to 0.15～0.3Mpag; Regulate regeneration cycle compressor (K-102) and be exported to the pipeline valve (manual bypass) that burns jar (D-102), require down so that the outlet pressure of regeneration cycle compressor (K-102) satisfies equipment, the systemic circulation amount is carried gradually to maximum (regeneration cycle compressor K-102 design load 10000～12200Nm
3/ h).
3). with blind plate 5 this part pipeline nitrogen replacement of reactive moieties and E-102 shell side outlet line, go out the interior feedstock oil of reactor by burning jar (D-102) jar undercutting simultaneously to hypomere control valve 4 to reactor.Must guarantee that system's nitrogen replacement is qualified, not contain feedstock oil.
4). heating furnace (F-101) begins heating; And burn condition (following table) according to catalyst regeneration and carry out.
The catalyst in-situ regeneration burns condition
| Operating procedure | Temperature, ℃ | Operating time, h | Heating rate, ℃/h | Oxygen content, v% | The operation medium |
| Heat up | Normal temperature～400 | 8 | 25 | 0 | High nitrogen |
| Constant temperature burns | 400 | 120 | 0.5 | High nitrogen+air | |
| Constant temperature burns | 400 | 0.5~21 | High nitrogen+air | ||
| Heat up | 400～450 | 2 | 25 | 21 | Air |
| Constant temperature burns | 450 | 21 | Air | ||
| Cooling | 450～250 | 6 | 33 | 21 | Air |
5) in the burning process as required, mend into air and regulate its flow of control to regeneration cycle compressor (K-102) porch and reactor hypomere bed, be strictly on guard against temperature rise too fast or too high (high some temperature is controlled at 450 ℃～470 ℃, definitely can not above 470 ℃); Burn jar (D-102) tank deck by adjusting simultaneously and burn O in emptying control valve control system pressure and the circulating air
2Concentration.
6), progressively go into amount and improve the temperature of underpaying in the reactor by the benefit that improve to purify wind and non-purification wind according to reactor bed temperature rise situation; Guarantee 50～60 ℃ of bed temperature rises (temperature difference in the reactor between each section ground floor and the 3rd layer), maximum temperature is lower than 470 ℃ in the reactor; If sulfur content is higher in the catalyst carbon deposit, then need to mend alkali lye to burning (D-102), to reduce the sulfide content in the circulating air by interim pipeline.
7) reach 440～450 ℃ (the peak temperature stage of reaction in) when feeding a large amount of air and burning temperature, and bed has not had obvious temperature rise, constant temperature stops bubbling air after four to five hours, and employing N2 replaces O to the reactor
2Content then burnt end less than 0.5% o'clock.
8) reduce heating furnace (F-101) outlet temperature gradually, make reactor batch temperature reduce to 240 ℃～250 ℃, cooling rate＜50 ℃/h.
9) after qualified, change relevant blind plate, off-response device terminal valve is opened the by-pass valve, and reactor is standby.
Of the present utility model as follows with contrast effect prior art:
Transform forward and backward regeneration contrast of the temperature variations in the reactor when burning
(with the 4th, six cycles as relatively):
| Project | The accumulative total used time (h) before transforming | Transform the back accumulative total used time (h) |
| In the reactor epimere ground floor begin to burn～410 ℃ | 59 | 44 |
| In the reactor epimere second layer begin to burn～410 ℃ | 150 | 75 |
| In the reactor the 3rd layer of epimere begin to burn～410 ℃ | 187 | 115 |
| In the reactor stage casing ground floor begin to burn～410 ℃ | 187 | 115 |
| In the reactor stage casing second layer begin to burn～410 ℃ | 226 | 133 |
| In the reactor the 3rd layer in stage casing begin to burn～410 ℃ | 269 | 159 |
| In the reactor hypomere ground floor begin to burn～410 ℃ | 269 | 159 |
| In the reactor hypomere second layer begin to burn～410 ℃ | 310 | 167 |
| In the reactor the 3rd layer of hypomere begin to burn～410 ℃ | 356 | 193 |
Regeneration is burnt and is transformed forward and backward effect:
Improved system not only makes the time of burning shorten 3 days, KWh surplus the saves energy about 3.3 ten thousand, and nearly 20,000 tons of economized cycle water has also been saved a large amount of fuel gas and N2 simultaneously, for my company energy-saving and cost-reducing made outstanding contribution, detail as per following table:
1, transforms forward and backward regeneration and burn used time contrast
2, transform forward and backward consumption contrast (with fourth, fifth cycle as relatively)
| Consume | Before the transformation | After the transformation | Relatively | |
| 1 | Recirculated water | 100322t | 81512t | -18810t |
| 2 | Electricity | 165960KW.h | 143832KW.h | -33192KW.h |
| 3 | Nitrogen | 5.63t | 4.6t | -1.03t |
| 4 | Steam | 130t | 83t | -47t |
| 5 | Fuel gas | 5.13t | 3.47t | -1.66t |
| 6 | Fresh water | 67t | 40t | -27t |
| 7 | Wind | 47.4KNM3 | 36.9KNM3 | -10.1KNM3 |
Obtain on the basis of preliminary effect the method that the period 6 adopts two-way to burn from the beginning in the period 5; And burn one tunnel non-purification wind porch increase, one buffering wind jar from advancing reactor, played the effect of excising most water, dust and buffering.Contain the harmful effect of low amounts of water in the non-purification wind thereby solved, the effect that new technology is burnt regeneration is embodied most vividly catalyst.Detail as per following table:
Burn through test that the cycle has shortened 5 days again on the time ratio period 6, KW.h, recirculated water about 3.1 ten thousand tons and a large amount of fuel gas and nitrogen surplus the saves energy 5.5 ten thousand, calculate with the refining amount of heavy carbon four 5.5t/h of naphtha 5.4t/h simultaneously, but the multi-processing naphtha is 648 tons again, 4 660 tons in heavy carbon, ton surplus many production cleaning component oil 745, about 565 tons of motor liquified gas is for our company has created huge economic benefit.
Claims (1)
1. the device of a charring straight-run gasoline gasoline upgrading catalyst regeneration, comprise reactor (R-101), heating furnace (F-101), heat exchanger, air cooler (A-101), cooler (E-104), gas compressor with reciprocating (K-102), burn jar (D-102), non-purification wind drain sump (D-113), control valve and reactor (R-101), direct steaming gasoline non-hydrogen modifying apparatus reactive moieties regeneration gas compressor (K-102) suction line is provided with an air intake and burns pipeline, one end of pipeline is arranged on the suction line of regeneration gas compressor (K-102), and the other end links to each other with purification wind house steward; It is characterized in that heat exchanger (E-102) outlet line is provided with non-purification wind drain sump (D-113), burning pipeline with air intake is connected, pipeline one end is drawn a pipeline and is linked to each other with the middle part of non-purification wind drain sump (D-113) from installing the total pipeline of original non-purification wind, draw a pipeline links to each other with heat exchanger (E-102) shell side outlet line from the top of non-purification wind drain sump (D-113), under the control of the hypomere C4 charging control valve of reactor (R-101), non-purification wind enters reactor (R-101).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200820074042XU CN201192639Y (en) | 2008-03-11 | 2008-03-11 | Catalyst coke burning regeneration apparatus for straight-run gasoline non-hydrogenation upgrading process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200820074042XU CN201192639Y (en) | 2008-03-11 | 2008-03-11 | Catalyst coke burning regeneration apparatus for straight-run gasoline non-hydrogenation upgrading process |
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| Publication Number | Publication Date |
|---|---|
| CN201192639Y true CN201192639Y (en) | 2009-02-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU200820074042XU Expired - Fee Related CN201192639Y (en) | 2008-03-11 | 2008-03-11 | Catalyst coke burning regeneration apparatus for straight-run gasoline non-hydrogenation upgrading process |
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| Country | Link |
|---|---|
| CN (1) | CN201192639Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101244395B (en) * | 2008-03-11 | 2011-04-27 | 蓝星石化有限公司天津石油化工厂 | Device for regeneration and charring of straight-run gasoline gasoline non-hydro modified catalyst |
| CN109456137A (en) * | 2018-11-01 | 2019-03-12 | 国家能源投资集团有限责任公司 | Methanol to olefins reaction-regeneration system stops start-up method |
-
2008
- 2008-03-11 CN CNU200820074042XU patent/CN201192639Y/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101244395B (en) * | 2008-03-11 | 2011-04-27 | 蓝星石化有限公司天津石油化工厂 | Device for regeneration and charring of straight-run gasoline gasoline non-hydro modified catalyst |
| CN109456137A (en) * | 2018-11-01 | 2019-03-12 | 国家能源投资集团有限责任公司 | Methanol to olefins reaction-regeneration system stops start-up method |
| CN109456137B (en) * | 2018-11-01 | 2021-03-02 | 国家能源投资集团有限责任公司 | Work stopping and starting method of methanol-to-olefin reaction-regeneration system |
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Granted publication date: 20090211 Termination date: 20130311 |