JPS60137993A - Method of generating fuel gas for thermal decomposition - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention is disclosed in U.S. Patent No. 1 to McKinlley W.
I, 061. ! '1ci26 and No. 4.097.36
No. 3, the disclosure of which is hereby incorporated by reference.

More particularly, the present invention provides a C1
An improved fuel gas generation system for solid state heating is provided.

This invention is related! The method of decontamination is specifically explained in the environment of a conventional regenerative pyrolysis reactor (TRC) as an example FIIi' in FIG.

Referring to FIG. 1, in the prior art -r RC process system C, the pyrolysis feedstock or residual oil is heated to 1 to 1.
Small v°9 (Mix the gas L, : is the blend L! J-,
) The hydrogen passes through line 12 through hydrogen to sulfur zone 1 or 14. Hydrogen sulfide effluent gas passes through line 16 and enters flash ff, 18, where it enters hydrogen sulfide and hydrogen sulfide. Contaminated gas (light gas) containing hydrogen sulfide passes through line 20 (head soil (removal, Meanwhile, the flash liquid is removed through the inlet 22. The flash liquid passes through the preheater 24, mixes with dilution vapor entering through line 26, and then passes through line 30.
C flows to the bottom of the pyrolysis reactor 28.

The hot regenerated solids stream is charged through line 32 and enters through line 34 before entering the upper back pipe 28!
Combine with water vapor or other fluidizing gas at t1M. Oil, water vapor, and hot solids are entrained (flowing in the -L direction through the riser pipe 28 and exiting through the curved segment 36 at the top of the I-f pipe). h Avoid inducing centrifugation of the affected solids. The flow containing the bulk of the body passes through the upper boundary discharge section 38 and, if desired,
Solid content 111-S I/Ripper-Proceed to 42 1) From 11
2 through twin 40 (entering A1 to mix with soil solids). Another stream containing the bulk of the product passes through conduit 44 (axially 4 Jl out). solid content ml
"Enter through line 46 in front of Stritzbar 48"
The negative Nl can be reduced by means of a quenching flow.

Stripper water quality is through Larn 50 and 52)
- C solid dividers 42 and 48 are charged respectively. The product stream is removed from solid fractions 111, 42 and 48 through lines 54 and 56, respectively, and line 5.
8 and passed through secondary quenching and oxalate recovery equipment (not shown). The solid coke that has arrived at 41 passes through lines 60J3 and 62 and solids N1 vessels 42 and 48
and are combined in a line 64 passing through the -1-x barno. If desired, 1--thi oil can be added to burnout 66 through line 68 while stripping steam is added via rain 70 to strip the combustion gases from the heated solids.

Air can be added to the C burner through line 69. The combustion gases are hot removed from the C barb through line 72 for passage to 13 and an energy recovery system (not shown), containing 1,
1 ton of mountainous thermal solid? I) Remove the burner via line 32 to avoid circulation to tube 28. In order to cover the production of acid, petroleum residue is added to hydrogen (r ri (1'3) (,650
T O J, and 900 N two) 1111 general smell r1
g through a catalytic hydrodesulfurization zone and combine the hydrogen with the oil during the hydrogen circulation stage. The hydrogen 11;2 sulfur residue acts as a heat source with entrained inert heat residue and diluent gas at a temperature between about 1300 and 2500 T and about 0.
During the intervening time from 0.5 to 2 seconds, it passes through a pyrolysis zone to produce decomposition products and ethylene and hydrogen. For the production of ethylene by pyrolysis, a hydrogen feedstock, at least b
00 volume t1% at 400 ° I: 1141 is a hydrocarbon source containing light gases of crude oil boiling between 400 °
Avoid passing through the decomposition zone during the bath time between 0' and 2500° for 0.05 to 2 seconds; the hand-lift ratio of gas to fuel oil is at least 0.3 But, same 11!I
The severity of the decomposition is 1/1 + 'RFT note 1J refueling: 11th and C a little 'Ku and 612 monkeys Q1% methane yield to 3
Jioru. When entering the decomposition zone 1, the product 13
00 King J, it is also quenched to a low temperature, but on a dosage basis, the ethylene yield is greater than the methane yield.

FIG. 2 illustrates the improved method J3 and system of the present invention that would be implemented in place of coke burner no. 06 (FIG. 1) in the prior art TRC system.

Particulate solids and hydrocarbon feed gas are 11Δ and 12A
and enters the tubular reactor 13A through the respective lines. The effluent from tubular reactor 13Δ is separated from particulate matter in divider 14Δ and quenched in line 15Δ by quenching material injected from line 17A. Separate spilled material! , two solids are sent to the solids separator through line 16Δ. The remaining solids are sent to the quenched product gas in the second separator R1 18△ (sent to the solid stripper 22A). Take it out.

The particulate solids in the solid stripper 22Δ are removed from the tubular reactor 1
Heat is distributed during the pyrolysis in 3Δ, but must be reheated and converted into a tubular reactor 13A to continue the cracking process.

The particulate solids are stripped by steam delivered through line 23A to solids stripper 22A (gas in solids stripper 27A) before being reheated.

After stripping the solid or gaseous impurities in the solid stripper 22△, the particulate solid has a temperature of about 1450 °C.

The combustion vessel 30A of the present invention is a combustion vessel 30A.
, and fuel, air (or oxygen) J5 and preheating to steam 1 ml 1 blue, these b are combustion vessels 30
It will be distributed to △. Preheater 32△, 34AJ5 and 36A
are shown in the fuel line 38A, air line 40AJ, and steam line 42Δ, respectively.

The system also includes a transfer train 44Δ into which the combusted fuel residue from combustion vessel 30Δ and stripped particulate solids from solids stripper 22A are combined to heat and heat the particulate solids. The transfer line 44Δ provides sufficient intervening time for the water vapor emanating from the combustion vessel 30Δ, allowing the presence of hydrogen to decompose -C by reaction with carbon. and remove net carbon from the solid-gas mixture. Desirable real mrl! As for the smell C, the transfer line 44A is about 100
-Feet no 1 (Za C Aro・). Line 26.DELTA. may be provided with pneumatic transport gas if necessary.

The N1 reactor 46Δ, such as the reactor 1-1 reactor 1-1, is provided for heating and separating the granular solids from the fuel gas. part N (particulate solids from vessel 46Δ are returned to hot solids container 27Δ through line 48Δ and -
CvA1 gas is taken out to the head through line 50A.

In one culm, fuel fil, air J3 and water vapor are passed through lines 38A, 408 and 42A respectively to combustion vessel 30A.
and combusted therein at a temperature of about 2300° to produce a fuel gas having a high ratio of CO to CO2 and an equimolar ratio of at least 120 to 1-12. 1+20 s of combustion gas leaving the combustion vessel 30A41)
In the presence of hydrogen, the fuel gas is mixed into the granular solids at a ratio of 13 to the ratio required to react with carbon and decompose water vapor. This ensures that the net carbon will be removed before reaching separator 46Δ.

The combustible gas from the combustion vessel 30A with a temperature of about 23001=C is about 1/1 in the tubular vessel 44Δ. Mix the wet IQ of b with the stripped granular solid.

The particulate solids and the fuel gas rapidly reach an equilibrium temperature of 17ε30'I- and continue to pass through the tubular vessel 44A.

During passage through tubular vessel 44A, the particulate solid-fuel gas mixture provides the necessary heat for the i[taste coke in the mixture to react with the water vapor. As a result, the granular solid-fuel scum mixture is cooled by about 30'r, i.e. from 1780 to 17
Cool to 50'F.

The ladle-shaped solid-fuel scum mixture is in the separator 4θΔ (min. 11
11. L, and the fuel waste is taken out through the 1750'F'r line 50△. The granular solids are fed at a temperature of 1750° and then transferred to a tubular reactor 1
It reaches 3Δ.

In one embodiment of the razor of the present invention, as illustrated in FIG. 33, fuel and air are fed into a combustion vessel 30Δ and burned to a temperature of about 2,300° C. to give fuel scum. 23
The fuel gas below 0.00°C and the particulate solids below about 1450°C mix in transfer line 44A at a temperature of about 1/186°C.

Air is then sent through line 54Δ to transfer line 44Δ. The combustible F1 gas in line 44A is combusted to raise the humidity of the particulate solids to about 1750'F. The resulting flue gas is separated from the hot solids in separator 4θΔ and exits through line 52Δ. Hot granular solid [,1
Provides reaction heat that is returned to the system. Note that 38A indicates the fuel supply, and 40Δ indicates the air supply.

An example of the system i1J J: in Figure 3 is as follows: f
UII: 'i7000 bond fuel is preheated to 600°1 in preheater 32Δ and 1000' [2VMS CF+] air is heated to 2 in combustor 30Δ.
Burn under 300 ("S U 15, C3MM SC
F l) generates fuel gas.

2300 T'dJ of 15 M M S CF I)
IP! The 11 grains of granular material mixed with the 11-grain stripper 22 Δ, which transfers the stone gas, removes 1,600 bonds per hour of carbon deposited on the soil.Synthesized fuel gas-granular solid gas mixture is 515 within about 5 milliseconds
An equilibrium temperature of 1480'F is reached at 1 g. After that, 13MM SCI+) of air was sent to the transfer twin 44A, and at 15.6MMS, the FD fuel i+1 gas was burned with the air to raise the solid temperature to 1750'F. Burn off the carbon in the bond.

The combustion residue from transfer line 44A separates from the solids in separator 46 and exits as a flue.

Although what is believed to be a preferred embodiment of the present invention has been described, the basic concept of the invention has been described. However, it is within the spirit and scope of the present invention, not only the embodiments, but also the scope of claim 1110J, which is within the spirit and scope of the present invention. It is intended to be interpreted to include variations and modifications thereto.

FIG. 1 is a schematic diagram of a T RC system and T culm according to the prior art.

This is a schematic diagram of the second drawer 31, the combustion 1'il gas generation system a-3 and the culm of this Bonmei.

Figure 3 is another law fruit/I! ! I show an example in which 0 gas and 5 additional heat are added to the granular solid.
I can do it.

Agent Ko Asamura Engraving of the drawing (no changes to the content) Continued from page 1 Johnson Jamin Roadney North Babylon, York State, Pen 67 Procedural amendment (method) % formula % 1. Indication of the case Showa! 7 year patent application No. 72JF? //Relationship with item 3, party making the amendment 1'l Special g゛"Applicant 5, the date of the amendment order A16, Supplement 1, the number of inventions increases from this date

Claims (1)

[Claims] <1) The temperature within the decomposition zone is 1300° and 2500'
', where the hydrocarbon feedstock or hydrogen sulfided residue is entrained with an inert 1!L solid a5 min with a diluent gas with an intervening time of up to 0.05 or C52 seconds.
In the TRC process (i5), the generation of fuel gas and the coke removal step on the solids are carried out by a) high ratios of Co to 0.02 and from 1 to 120 to 112 from the fuel, air and steam. generating a fuel gas with a high molar ratio; 1) distributing the fuel gas to a tubular transfer line;
d) mixing the fuel gas and the particulate solids until an equilibrium temperature is reached; and C) discharging heat from the particulate solids-fuel gas mixture. J to water vapor
: An improved method consisting of removing -''-cus from a granular solid. (2) The granular solid is passed along with the 11th scum at a container width of about 100 noy 1-1/sec, and L nl, ! A method according to claim 1, wherein the I-coke reaction reduces the consumption of particulate solids-fuel scum. (3) Burning the fuel gas in the transfer line to further heat the solid and remove the gas from the solid.
The method according to claim 1), further comprising the step of: (4) The temperature in the ζ band is 1300' and 250
0 'I- and there (') The hydrocarbon feedstock or hydrogen sulfided residue passes through the cracking zone with entrained inert solids d3 and diluted scum with a residence time of from 0.05 to 2 seconds. A3 in the fRC method (, fuel gas generation J3
and the process of removing the sludge on the solid, a) removing the fuel scum from the fuel J5 and air; 1)
) Dispense the fuel scum to the transfer line;
- d) Burning the fuel gas in the transfer line to raise the temperature of the solid to remove coke from the solid. (5) Preheat the fuel to 600°C and the air to 1000'F; combust the preheated fuel at 7000°F and the air at 13MM 5CFD to generate fuel gas for delivery to the transfer line, where 13M
4. The method of claim 2, further comprising the step of distributing air in the MSCI'-D to the transfer line to facilitate combustion of the fuel gas flowing into the C transfer line. (6) The temperature in the cracking zone is between 1300 and below 2500°C, where the hydrocarbon feedstock or hydrodesulfurized residue is combined with the entrained inert solid rice diluent gas at 0.05°C.
Capture interval J, i interval C decomposition from to 2 seconds? J3 on the 1st Rc system passing through the IIP area, a) Fuel gas, air i13
1τ' of 2°% l112! Burn a small ratio and emit 1 gas! 1. b) a transfer line; and C) means for mixing the fuel gas and the particulate solids in the transfer line, whereby the fuel gas, by intimate contact therewith, lowers the temperature of the particulate solids to reduce the water vapor in the fuel gas. An improved system for heating and removing coke from granular solids comprising covering the solids with coke removal during movement through said transfer line. (7) The system of claim (6), further comprising means for heating the solids to clean the coke and then heating the solids to separate the burnt gas from the granular solids. (8)a, CO vs. CO from fuel, air JjJ, and water vapor
generating a fuel gas having a ratio of 2 and a high molar ratio of 1120 to 112; b. distributing the fuel gas to a tubular transfer line;
d. Mix the fuel gas and the granular solids to reach equilibrium 1α; A method of generating combustion gas and removing coke deposited on the solids comprising removing coke from particulate solids by heat and water vapor from a +1 gas mixture. (9) GOO King preheated 6500 bond/fuel, preheated to 1000″F 114.MMSCID air and 72400 bond preheated to 1000 tons/
The water vapor of time is burned to 2300°F! (The method described in claim box 1711, item (8)).
The feature that the equilibrium temperature of the particulate solid-fuel gas mixture is 1780'F at a temperature of 1780'F
11. The method described in paragraph (8). (11) Burning granular solids1'! Approximately 100 noi in the container per gas tube in 1-7 seconds is 1ffi? The hydrothermal air coke reaction that decokes the particulate solids by combustion. degree 1780'F
l) 'et al. 1750T': 'FL, j method according to claim (10). (12) As a result, 1 gas of 41-ji is approximately 100B
The method according to claim 9, wherein the BTU value of l-U/SCF is 41. (13) Particulate solid-fuel gas d? , about 5.0 milliseconds for the compound to reach equilibrium temperature. III) Toumasuke OJ:
11. The method of claim 10, further comprising a residence time of about 1 second for steam decoking the particulate solids. (14) Fuel consumption per gas is 8.9 moJ and %1-12.1
8.2-Ele% CO19,5Lle% CO'2.11
．． 7 mol% t-l 20 J: and 51,7 mol% N
The method according to claim (9), having a composition of 2. 15. The method of claim 8, further comprising the step of combusting the fuel gas in the transfer line to further heat the solids and remove coke from the solids. (16) a, fuel H'A d3 J, and generating fuel gas from air I! : b. Burn it gas into the transfer line; mix the C9 particulate solid with the fuel gas in the transfer line to increase the temperature of the solid 1α; and (1. Burn the fuel gas in the transfer line to increase the temperature of the solid ?F+
A. A method of heating a particulate solid and removing coke from the solid prior to dispensing the solid to a thermal reaction chamber, the method comprising increasing A19 to remove coke from the solid. (17) The fuel gas to be transferred and distributed to the inn is 2300 yen.
If the overlying particulate solids mixed with the fuel gas are at a temperature of 1450'F, the equilibrium temperature of the fuel gas-solids mixture is about 14861-C, and the fuel gas in the transfer line is The combustion of will raise the temperature of the solid to 17
Claim No. ('I 6 ) J
The method described in rI. (18) Fuel to 600'F and Air to +00
Preheat to 0'I; 7000 volts/n, 10)T
The heated fuel and air of 13MM 5CI-1) are combusted to generate fuel gas for delivery to the transfer line and the air of 13MM SCI"'D is transferred thereto.
The method of claim 16, further comprising the step of promoting combustion of the combustion gas in the transfer line by distributing the fuel into the transfer line. (19) a. Fuel, air and water vapor. Generates a fuel gas with a high molar ratio of 1 to 12° to 1-12.
Stage: b, transfer line; and CO fuel gas and particulate solids mixed in the transfer line -
means for heating the particulate solids so that the fuel gas increases the temperature of the solids by intimate contact therewith and the water vapor in the fuel gas removes coke from the solids while traveling through the transfer line. A system that removes coke. 20. The system of claim 19, wherein the transfer line is about 100 feet long. (21) The system according to claim (19), further comprising means for heating the I+ solid and removing the 1-x, and then separating the fuel gas from the heated granular solid. (22) Feature n'l' further comprising means for introducing air into the transfer line 7j according to claim (20)
Law.