Method of speeded down carbonization

FIELD: .oil industry

SUBSTANCE: method comprises preliminary heating of initial raw material, mixing it with the carbonization gas oil, supplying the mixture to the intermediate tank, heating the raw material up to the temperature of carbonization, and carbonizing it in the carbonization chamber to produce carbon and carbonization distiller. The distiller is supplied to the bottom section of the rectification tower in which it is separated into gas, gasoline, and light and cubic carbonization gas oils. The other heated hydrocarbon raw material is additionally supplied to the bottom section of the rectification tower. The concentration of sulfur in the material is higher than that in the initial raw material . The cubic gas from the rectification tower is carbonized by a known method to produce coke and distiller which is supplied to the bottom section of the rectification tower. The initial raw material can be mixed with the light or heavy carbonization gas oil.

EFFECT: simplified method.

2 cl, 2 tbl, 7 ex

 

The invention relates to the refining sector, particularly to a method and a delayed coking unit with possibility of simultaneous receipt of chars of different quality on a single installation.

The known method a delayed coking unit, in accordance with which the heavy oil residue (tar) is heated to a temperature of ˜350°and served in the lower part of the distillation column where it is mixed with the products of coking, coming from the coking chamber. The mixture of raw materials with recirculator (secondary raw material) is heated to a temperature coking˜500° (C) and served in one of the two alternately operating coke oven chambers with the formation of coke and coking products (Sahmetov. The technology of deep processing of oil and gas. - Ufa: Gil, 2002, str).

The disadvantage of this method is, first, the complexity of the regulation of the recirculation ratio, i.e. the ratio of the number of recirculating factions involved in the coking of the mixture with the primary raw material, and, secondly, cannot simultaneously receive on a single installation of different quality of chars in the case of, for example, processing at the plant sulfur and low-sulfur crude oils.

Usually in this situation, use two delayed coking unit, one of which uses sulfur raw materials with the receiving member is oxa for the aluminium industry, on the other - low-sulfur raw materials to receipt of needle coke for graphite electrodes. The manufacture and operation of two units of a delayed coking unit, working on various kinds of raw materials, cost of technology increases energy consumption, complicates the control system increases the number of maintenance personnel. Many of these shortcomings will not take place or their impact lessened production of two types of petroleum coke on one of the delayed coking unit. This reduces the number of personnel, reduced energy consumption, creates a unified management system, etc.

The known method a delayed coking unit, which consists in the fact that the raw materials are heavy hydrocarbon oil is mixed with a side stream of coke distillation column, having a boiling point of 168-454°C, heated and served in an interim capacity, connected in pairs with a distillation column, from the intermediate tank raw material mixture is sent to the coke oven where it is heated to a temperature of coking and then subjected to carbonization to obtain coke and coking distillate, which is then served in the lower part of the distillation column (Patent RF №1627088, SW 55/00, 1991).

However, this method also does not allow you to get on the same mustache is the time at the same time different in quality cokes.

The known method for delayed coking, one installation of two types of oil raw materials to produce needle coke of different quality (Copyright certificate №1810374, SW 55/00, 1993).

However, the rigidity of the technology of this method and the complexity of the possible manifestations of the properties of raw materials in the case of coking heavy petroleum residue (tar)with different sulfur content, does not ensure receipt of chars with different sulfur content in the case of coking sulfur and low-sulfur tars.

Closest to the claimed object is a process for delayed coking, including preheating of the feedstock, offset it with heavy oil coking, or resin pyrolysis, or heavy gas oil catalytic cracking, the feed mixture in the intermediate tank connected but couples with a distillation column, a secondary heating of the raw material mixture from the intermediate container in a coke oven to a temperature of coking and feed it into one of the reactors of coking. Distillate products of coking on the top of the reactor is directed to a distillation column where it is separated into gas, gasoline, light, heavy and CBM gas oils and derived products derive from the installation. This method can be carried out on two-, three - or chetyrekhsektornoi scheme (Patent RF №2206595, SW 55/00, 2003).

Fault is m this way, like other well-known, is the lack of efficiency, the impossibility of simultaneous processing of low-sulphur and high-sulphur raw materials to produce coke of different quality.

Object of the invention is to enhance the functionality of the method, increasing the flexibility of the technology and improve the quality of coke.

To solve this problem is proposed a method for delayed coking, including preheating of the feedstock, mixing it with the oil coking, the flow of the mixture in the intermediate tank connected in pairs with a distillation column, heating the raw material mixture from the intermediate container in a coke oven to a temperature of coking and coking in the coking chamber with getting coke and coking distillate, which is served in the lower part of the distillation column where it is separated into gas, gasoline, light, heavy and CBM oil coking, in which according to the invention in the lower part of the distillation column additionally serves more heated hydrocarbon feedstock with a higher sulfur content than the initial raw material, and CBM gas from the distillation column is subjected to coking in a known manner with the receipt of coke and coking distillate, which is served in the lower part of the distillation column.

The original seriesspecial with a light or heavy oil coking, taken in an amount of 10-100% load raw materials and feedstock use tar, sweet crude, distillate cracking residue or heavy gas oil catalytic cracking.

When used as a feedstock oil sweet crude oil obtained low-sulfur coke for the aluminum industry, and in the case of distillate cracking-residue or heavy gas oil catalytic cracking needle coke for electrode industry.

The method is as follows.

Raw materials (I), such as tar, sweet crude, distillate cracking residue or heavy catalytic cracking gas oil is heated in a furnace or in heat exchangers due to the heat of the exhaust products of coking temperatures of ˜350°C, mixed with a slight (II) or severe (III) oil coking and served in an interim capacity of 1, resulting in a secondary raw material, which is heated in the furnace 2 to a temperature of coking ˜500°and sent to one of the two alternately operating coke oven chambers 3 the first block. Formed in the coking chambers 3 coking distillate (IV) direct in the bottom part of the distillation column 4, in which the fractionation boiling fractions of the distillate coking with the formation of gas + gasoline (V), light, heavy the th and CC (VI) of the oil coking.

Hydrocarbons (VII) with a higher sulfur content than the initial raw material, such as tar sour crude oil, after heating in a furnace or in heat exchangers due to the heat of the exhaust products of coking temperature ˜350°served in the lower part of the distillation column 4, where it is mixed with the condensation products taglocity fractions of distillates coking coming into the distillation column from all the coke chambers 3 and 6. CBM gasoil coking from a bottom of the distillation column is heated in the furnace 5 to the temperature coking˜500° (C) and sent to the other two coke oven chamber 6 of the second unit.

Formed in the coking chambers 6 coking distillate (VIII) is also sent to the main distillation column 4. Figure 1. presents the scheme of the proposed method

The method is illustrated by the following examples. Characteristics of raw materials and components coking shown in table 1. The material balance and the characteristics of the resulting chars are given in table 2.

Example 1 (known way). In accordance with a known method is carried out gumming different kinds of raw materials, the characteristics of which are given in table. 1. Coking is performed on industrial double, i.e. having 4 coke oven chambers, the delayed coking unit with the presence of prom is mediate capacity.

Feedstock mixture (1:1) tars low-sulfur and sulfur crude oil is heated in a furnace to a temperature of ˜350°C, mixed with 10% of the raw material, the cubic of gas oil (heavy recirculator) from the bottom of the distillation column and sent to a buffer tank connected in pairs with the main distillation column. From the bottom of the intermediate tank feedstock is mixed with heavy recirculator is supplied into the reaction furnace, where it is heated to a temperature 495-505°and enters one of the alternately operating coke oven chambers of the first and second blocks. Formed coke coke accumulates in the cells, and the distillate coking on shlemovoy the pipe enters the bottom part of the distillation column where it is divided into gas, gasoline, light, heavy and CBM gasoil. Part of the cubic gasoil, as mentioned above, is directed to the mixing with the feedstock, and the excess output from the installation.

According to this way of engaging in raw material, even heavy risaykl does not significantly increase the yield of coke, and increasing the rate of recycling, i.e. the increase in the proportion of risaykl in raw materials, reduces plant capacity by feedstock and increases energy costs.

Example 2 (the proposed method). Tar, sweet crude is mixed with 10% heavy oil coking supplied from battery OS is the ESD of the distillation column, the resulting mixture was fed into the intermediate tank 1. The residue from the bottom of the tank 1 is heated in the furnace 2 to a temperature of coking 500°and served in one of the two alternately operating coke oven chambers 3 of the first unit to receive coke and coking distillate, which enters the distillation column 4, where it is separated into gas + gasoline, light, heavy and CBM oil coking.

Tar sulfur oil is heated to a temperature of 350°and served in the lower part of the distillation column 4, where it is mixed with magelonidae fractions of distillate coking and how CBM gasoil from a bottom of the distillation column 4 is fed into the furnace 5, where it is heated to a temperature of coking 500°and from the coke oven comes in the other two alternately operating a coke oven chamber 6 of the second unit with getting coke and coking distillate, which then enters the distillation column 4 to the separation.

As is seen in table 2 the data on the first block of the delayed Coker receive low-sulfur coke, fully satisfying the regulatory requirements of GOST 22898-78. The second unit receives sulfur coke.

Thus, this example shows that the proposed method for delayed coking different sulfur content of raw materials allows to obtain on a single installation of two VI is and coke, including sulphur, while the coking mixture of tars by a known method get sulfur coke with a high content of vanadium and, consequently, unsuitable for use in the aluminum industry.

Example 3 (proposed and fashion).

The method is carried out analogously to example 2, but with the difference that the tar sweet crude oil before serving in the intermediate tank of pre-mix is not heavy, and with a light gas oil coking supplied from the rectifying column. And in this case was obtained two types of coke: sweet and sour.

Example 4 (the proposed method).

The method is carried out analogously to example 2, but with the difference that in feedstock use distillate cracking residue that was mixed with a 100% (1:1) heavy oil coking, and in the lower part of the distillation column serves tar, sweet crude.

As a result, the first power plant to get high-quality needle coke for electrode industry, and on the second block coke for the aluminum industry with a reduced content of sulfur and metals.

Example 5 (the proposed method).

The method is carried out analogously to example 4 with the difference that the distillate cracking residue before serving in the intermediate tank mix with 100% (1:1) light gas oil Kok is Finance.

In this case, we receive the first block of needle coke contains less sulfur, but at the same time the yield of coke is somewhat reduced.

Example 6 (the proposed method).

The method is carried out analogously to example 4 with the difference that in feedstock use decanoyl and in the lower part of the distillation column serves tar sulfur oil.

In this case, the first unit to receive the needle coke, and on the second block - sulfur coke.

Example 7 (the proposed method).

The method is carried out analogously to example 5 with the difference that in feedstock use decanoyl and in the lower part of the distillation column serves tar sulfur oil.

Thus, the above examples show that the proposed method a delayed coking unit allows to obtain simultaneously on a single installation valuable sweet anode coke for the aluminum industry, needle coke electrode for industry and sulfur coke. In the case of receiving needle coke method allows to improve its structure to increase the assessment of microstructure in points. Set out fairly in the claimed combination of different kinds of raw materials, which indicates the flexibility of the proposed method and extend its functionality.

Table 1
Characterization of raw materials and components coking
IndicesTar sweet crude oilTar sulfur oilDistillery cracking residueDecanoylThe oil coking
light (FR. 180-350°)heavy (FR. >350°)
Density, g/cm30,99341,02031,04091,04500,8577-0,87370,9341-0.9660
Cocking behavior, wt.%15,517,412,85,10,0-0,060,74-1,39
Sulfur content, wt.%1,283,840,540,60,90-2,901,20-3,30
Fractional composition:
temperature TC, °443390--202-210-
- 5% boils at, °47244528322 --
- 10% boils at, °489464317284220-
- 20% boils at, °503492381291--
- 30% boils at, °515-492318--
- 40% boils at, °---350--
- 50% boils at, °---378275-282-
- 60% boils at, °---391--
- 70% boils at, °---400--
- 80% boils at, °---438--
330-333-
- temperature QC °341-344-
Contents V%0,00420,024----
The Ni content,%0,00300,012----

Table 2
The material balance and the quality of chars
The known method example 1Examples of the proposed method
Example 2Example 3Example 4Example 5Example 6Example 7
The material balance
Taken, wt.%
- raw materials100100100100100 100100
Received, wt.%
- gas1010.2the 10.19,49,09,49,3
petrol10,710,910,7the 10.19,97,37,1
- light gasoilto 33.834,034,130,129,227,726,0
- heavy gasoil19,118,518,922,825,927,130,8
- Cox26,412,414,012,214,015,0 12,6the 13.412,614.4V14,1a 12.714,1
Total:100100100100100100100
The quality of coke
Content, wt.%
- sulphur2,821,384,041,34,040,661,120,521,120,804,00,564,0
vanadium0,05760,01340,0910of 0.01250,0910-0,0112-0,0112-0,0900-0,0900
- Nickel0,03180,01010,05020,00950,0502-0,00810,0081- 0,0500-0,0500
Evaluation of microstructure, score-----5,6-5,6-5,8-5,8-

1. The way a delayed coking unit, comprising mixing the feedstock with oil coking, the flow of the mixture in the intermediate tank connected in pairs with a distillation column, heating the raw material mixture from the intermediate container in a coke oven to a temperature of coking and coking in the coking chamber with getting coke and coking distillate, which is served in the lower part of the distillation column with getting gas, gasoline, light, heavy and VAT of oil coking, characterized in that the lower part of the distillation column additionally serves more heated hydrocarbon feedstock with a higher sulfur content than the initial raw material, and CBM gasoil from the distillation column is subjected to coking in a known manner with the receipt of coke and coking distillate, which is served in the lower part of the distillation column.

2. The method according to claim 1, characterized in that the feedstock is mixed with a light or heavy oil coking, taken in an amount of 10-100% of the raw material loading.

Cab according to claim 1, characterized in that the feedstock used tar, sweet crude, distillate cracking residue or heavy gas oil catalytic cracking.



 

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8 cl, 1 ex, 1 tbl, 1 dwg

FIELD: petroleum processing.

SUBSTANCE: invention aims at simultaneously producing petroleum coke with low and high contents of volatiles, which coke, after calcination, can be used to manufacture anodes or graphitized products. Process of producing petroleum coke through retarded coking of petroleum residues comprises supplying feedstock to coke chamber at 475-485°C, coking during 14 to 36 h, discharging resulting coke by drilling central well in the coke bulk and cutting coke of the top part of chamber until it is completely emptied at a depth 4-5 m, discharged coke is removed from under the chamber and after that cutting of coke is continued in the lower part of chamber until it is also completely emptied. Thereafter, coke discharged from the top part of chamber and coke discharged from the lower part of chamber are stored separately. The former contains at least 15% volatiles and is used as substitute of sintering and thinning components in coal coking charge in blast furnace coke production and the latter contains no more than 11% volatiles.

EFFECT: enabled simultaneous production of volatiles-rich and low-volatile cokes.

1 tbl

FIELD: .oil industry

SUBSTANCE: method comprises preliminary heating of initial raw material, mixing it with the carbonization gas oil, supplying the mixture to the intermediate tank, heating the raw material up to the temperature of carbonization, and carbonizing it in the carbonization chamber to produce carbon and carbonization distiller. The distiller is supplied to the bottom section of the rectification tower in which it is separated into gas, gasoline, and light and cubic carbonization gas oils. The other heated hydrocarbon raw material is additionally supplied to the bottom section of the rectification tower. The concentration of sulfur in the material is higher than that in the initial raw material . The cubic gas from the rectification tower is carbonized by a known method to produce coke and distiller which is supplied to the bottom section of the rectification tower. The initial raw material can be mixed with the light or heavy carbonization gas oil.

EFFECT: simplified method.

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FIELD: petroleum processing.

SUBSTANCE: invention relates to apparatuses for isolation of hydrocarbon fractions of liquid fuel and coke from straight-run goudron and acid sludges, aged mazuts, oil slimes, and can be used to utilize indicated wastes. Reactor for isolation of hydrocarbon fractions of liquid fuel and coke from subquality coking products and petroleum processing wastes comprises upright cylindrical body 1 with plane bottom 2 provided with external heater 3 having central opening 21 with connecting pipe 22; feedstock receiver 5 secured to drive shaft 4; perforated sparkling tube 6 rigidly connected to feedstock receiver 5; and knife 7 mounted on shaft 4 before sparkling tube in the direction of rotation of shaft 4 and in parallel to bottom 2 and tube 5. Perforations of sparkling tube 6 are made in the form of through grooves 11 along cylindrical surface of tube 6 and are positioned over plane gutter 12. Sparkling tube 6 bears rod 13 for longitudinal displacement. Rod 13 supports scrappers 16. Body 1 accommodates direct (9) and back (10) pushers of rod 13. Feedstock receiver 5 and sparkling tube 6 are provided with screens 24 and 25. Cutting edge of knife 7 is made in the form of equal-sided corner prominences. Hub 19 with radial inclined blades 20 is attached to lower part of shaft 4 and connecting pipe 22 is provided with radial counterblades.

EFFECT: prolonged duration of continuous operation of reactor and increased productivity.

3 dwg

FIELD: petroleum processing.

SUBSTANCE: method according to invention determines pressure gradients at exit and entrance in each section of the furnace and real gradient is compared to projected gradient, after which, depending on disagreement value, this value is diminished via variation of fuel consumption in corresponding furnace burner. Projected gradient is calculated using formula: ΔPi=k(L1+b)n, wherein ΔPi is pressure gradient in i-th section of coil, %; k, b, n are coefficients depending on conversion value, nature of raw material, and projected quality of final thermal destruction products; and L1 reduced length of coil from its beginning to i-th measurement point, %.

EFFECT: decreased coking of furnace coil and increased operation cycle of plant, which incorporates the furnace.

3 cl, 3 tbl

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