US Pat. No. 9,403,687

METHOD FOR PREPARATION OF AMORPHOUS SILICA FROM BIOMASS

WUHAN KAIDI ENGINEERING T...

1. A method for preparation of amorphous silica from biomass, the method comprising:
washing the biomass with 3 to 5 wt. % hydrochloric acid, sulfuric acid, or nitric acid, and drying the biomass;
after drying, pyrolyzing the biomass under anaerobic conditions to yield a pyrolysis gas and solid residues, collecting the
pyrolysis gas; and

calcining the solid residues in the presence of air to remove carbon residues and to yield amorphous silica.
US Pat. No. 9,388,091

CATALYST FOR METHANATION OF CARBON DIOXIDE, PREPARATION METHOD AND USAGE THEREOF

WUHAN KAIDI ENGINEERING T...

1. A catalyst for methanation of carbon dioxide, the catalyst being formed by mixing ash from a biomass power plant with a
nickel compound and calcining a resulting mixture, the catalyst comprising between 2 and 20 wt. % of nickel supported on a
second ash;
wherein:
the ash from the biomass power plant and the second ash comprise SiO2, Al2O3, CaO, Fe2O3,TiO2, MgO, and K2O; and

the catalyst is prepared according to a method comprising:
1) preparing an aqueous solution comprising between 5 and 30 wt. % of the nickel compound;
2) calcining the ash at a temperature of between 300 and 400° C. for between 20 and 40 min for removing combustible impurities
from the ash to obtain a second ash;

3) mixing the aqueous solution obtained in 1) with the second ash, and stiffing a resulting mixture for between 5 and 10 h
for uniformly impregnating the mixture;

4) desiccating the mixture obtained in 3) at a temperature of between 110 and 150° C. for between 0.5 and 1.5 h; and
5) calcining the mixture obtained in 4) at a temperature of between 400 and 500° C. for between 3 and 6 h to yield the catalyst.
US Pat. No. 9,255,225

METHOD FOR PREPARING LIQUID HYDROCARBONS FROM SYNGAS

Wuhan Kaidi Engineering T...

1. A method for preparing a liquid hydrocarbon from syngas, the method comprising:
1) mixing crude syngas from a biomass gasifier and a hydrogen-rich gas to yield a mixed gas, wherein a volume ratio of the
hydrogen-rich gas to the crude syngas is between 0.7 and 2.1;

2) removing moisture, carbon dioxide, sulfides, oxynitrides, and metal compounds from the mixed gas, and obtaining a fine
syngas;

3) introducing the fine syngas to a Fischer-Tropsch synthesis device for Fischer-Tropsch synthesis in the presence of a catalyst,
controlling a reaction temperature of the Fischer-Tropsch synthesis at between 150 and 300° C. and a reaction pressure of
between 2 and 4 MPa (A), to yield a liquid hydrocarbon; and

4) returning 70-95 vol. % of exhaust gases from the Fischer-Tropsch synthesis device to step 3) to mix with the fine syngas,
the exhaust gases comprising syngas, inert gas, and hydrocarbons, and introducing a resulting mixed gas to the Fischer-Tropsch
synthesis device.

US Pat. No. 9,409,775

METHOD OF PURIFICATION OF BIOMASS SYNGAS UNDER NEGATIVE PRESSURE

WUHAN KAIDI ENGINEERING T...

1. A method for purifying biomass syngas, comprising:
a) introducing syngas out of a gasifier via a top of the gasifier, through a water-cooling flue to a water-cooling quench
tower, where water is sprayed into the syngas for quenching slag;

b) introducing the syngas from the water-cooling quench tower to a waste heat boiler of a water-tube type to yield a first
vapor and a first cooled syngas having a temperature of 450±20° C.; introducing the first cooled syngas to a waste heat boiler
of a heat-tube type to yield a heavy tar, a second vapor, and a second cooled syngas having a temperature of 200±10° C.; and
supplying the first vapor and the second vapor to external devices;

c) washing the second cooled syngas in a Venturi scrubber in the absence of a filler to yield a first purified syngas;
d) introducing the first purified syngas from the Venturi scrubber to a wet electrical dust precipitator to yield a second
purified syngas for conducting dust removal and tar mist removal; and

e) extracting the second purified syngas by a coal gas draft fan, and transporting the second purified syngas to a wet gas
tank for storage or to a downstream process for use.

US Pat. No. 9,193,927

METHOD AND DEVICE FOR CONVERTING CARBON DIOXIDE IN FLUE GAS INTO NATURAL GAS

Wuhan Kaidi Engineering T...

1. A method for converting carbon dioxide in flue gas into natural gas using dump energy, the method comprising:
1) transforming and rectifying a voltage of dump energy generated from a renewable energy plant, introducing the voltage-transformed
and rectified dump energy into an electrolyte solution to electrolyze water therein to yield H2 and O2, and drying H2;

2) purifying industrial flue gas to separate CO2 therein and purifying CO2;

3) transporting H2 generated from step 1) and CO2 from step 2) to a synthesis equipment comprising at least two fixed bed reactors, allowing a methanation reaction between
H2 and CO2 to happen to yield a high-temperature mixed gas with main ingredients of CH4 and water vapor;

4) employing the high-temperature mixed gas generated from step 3) to conduct indirect heat exchange with process water to
yield superheated water vapor;

5) delivering the superheated water vapor generated from step 4) to a turbine to generate electric energy, and returning the
electric energy to step 1) for water electrolysis; and

6) condensing and drying the mixed gas in step 4) cooled through the indirect heat exchange, until natural gas with CH4 content up to the standard is obtained.

US Pat. No. 9,410,096

METHOD AND SYSTEM FOR COOLING AND WASHING BIOMASS SYNGAS

WUHAN KAIDI ENGINEERING T...

1. A system for cooling and washing biomass syngas, comprising:
a high temperature pyrolysis gasifier;
a water-cooling quench tower connected downstream to the gasifier via a water-cooling flue device;
a waste heat boiler, a scrubbing-cooling tower, and an electro-precipitator, all located downstream of the quench tower;
wherein water-cooling flue device comprises a water-cooling flue and the water-cooling flue is formed by an inlet water-cooling
flue, an upper-bend water-cooling flue, a straight water-cooling flue, a lower-bend water-cooling flue, and an outlet water-cooling
flue in series and sealed connection;

wherein the waste heat boiler comprises a water-pipe waste heat boiler and a heat-pipe waste heat boiler connected in series;
wherein the quench tower is connected to the waste heat boiler, the scrubbing-cooling tower, and the electro-precipitator
via syngas pipelines.

US Pat. No. 9,469,820

METHOD AND SYSTEM FOR RECYCLING CARBON DIOXIDE FROM BIOMASS GASIFICATION

WUHAN KAIDI ENGINEERING T...

1. A method of biomass gasification by utilizing carbon dioxide as a gasifying agent, the method comprising:
1) allowing the carbon dioxide to gasify biomass in a gasifier in the presence of external energy, whereby yielding syngas
comprising CO, CO2, CH4, H2, H2O, H2S, and COS;

2) cooling the syngas from 1) in a primary heat exchanger by using carbon dioxide as a cooling medium, whereby the carbon
dioxide is heated by the syngas to a temperature of between 350 and 600° C.;

3) cooling the syngas from 2) in a secondary heat exchanger by using water as a cooling medium whereby producing water vapor;
4) feeding carbon dioxide from 2) to the gasifier;
5) introducing the syngas from 3) to a cyclone separator and a gas scrubber for dust removal and purification;
6) contacting the syngas from 5) with the water vapor so that part of carbon monoxide in the syngas reacts with the water
vapor to produce hydrogen and carbon dioxide;

7) removing H2S and COS from the syngas from 6) to obtain a desulfurized syngas;

8) removing carbon dioxide from the desulfurized syngas to obtain a desulfurized and decarburized syngas;
9) introducing the desulfurized and decarburized syngas to a synthesizing tower, wherein the desulfurized and decarburized
syngas is catalyzed to yield oil and exhaust gas comprising carbon dioxide;

10) separating carbon dioxide from the exhaust gas from 9) to obtain an effluent gas free of carbon dioxide, and discharging
the effluent gas; and

11) introducing the carbon dioxide obtained in 8) and the carbon dioxide obtained in 10) to the primary heat exchanger as
the cooling medium.

US Pat. No. 9,255,226

METHOD FOR IMPROVING FISCHER-TROPSCH SYNTHESIS AND RECYCLING EXHAUST GASES THEREFROM

Wuhan Kaidi Engineering T...

1. A method of producing liquid hydrocarbons through Fischer-Tropsch synthesis, the method comprising:
1) subjecting a first syngas output from a biomass gasifier to a water-gas shift reaction and transforming part of CO in the
first syngas to CO2 and H2 in the presence of water to yield a second syngas, reducing a Fe-based or Co-based catalyst to yield an activated catalyst,
introducing the activated catalyst into a Fischer-Tropsch reactor, transporting the second syngas to the Fischer-Tropsch reactor
for Fischer-Tropsch synthesis in the presence of the activated catalyst, and controlling a reaction temperature of the Fischer-Tropsch
synthesis at between 150 and 300° C. and at a reaction pressure of between 2 and 4 MPa (A), to yield a liquid hydrocarbon
product and a first exhaust gas;

2) introducing the first exhaust gas to a first pressure-swing adsorber to recover hydrogen gas from the first exhaust gas,
obtaining hydrogen gas having a purity of 80-99 vol. % and a second exhaust gas, and dividing the hydrogen gas into three
feeds;

3) introducing the second exhaust gas to a second pressure-swing adsorber to recover methane from the second exhaust gas,
and obtaining methane having a purity of 80-95 vol. % and a third exhaust gas;

4) introducing methane to a methane reforming device, reforming methane in the methane reforming device to yield a third syngas;
5) returning the third syngas in step 4) and a first feed of the three feeds obtained in step 2) to step 1) to mix with the
first syngas and to adjust a hydrogen/carbon ratio of the first syngas, and obtaining a fourth syngas; and

6) returning a second feed of the three feeds obtained in step 2) to step 1) to reduce the Fe-based or Co-based catalyst.

US Pat. No. 9,249,358

METHOD AND SYSTEM FOR PRODUCING SYNTHESIS GAS

Wuhan Kaidi Engineering T...

1. A method for producing synthesis gas, comprising:
1) pre-processing a biomass raw material;
2) fast pyrolyzing the biomass raw material using a pyrolysis bed having a solid heat carrier to produce a product comprising
a pyrolysis gas, a carbon powder, and the solid heat carrier;

3) feeding the product obtained in step 2) to a cyclone separator and separating the pyrolysis gas from the carbon powder
and the solid heat carrier;

4) feeding the carbon powder and the solid heat carrier obtained in step 3) to a solid-solid separator and separating the
carbon powder from the solid heat carrier;

5) feeding the carbon powder obtained in step 4) to a carbon powder stock bin;
6) feeding the solid heat carrier obtained in step 4) to a carrier heating fluidized bed and heating the solid heat carrier,
and conveying the solid heat carrier to the pyrolysis bed for recycling use;

7) conducting spray, condensation with respect to the pyrolysis gas obtained in step 3) by using a condensate tank to produce
a biological fuel oil and a non-condensable pyrolysis gas;

8) pressurizing one part of the biological fuel oil obtained in step 7) by using a high pressure oil pump and feeding the
one part of the biological fuel oil to a gasification furnace to be gasified; and pressurizing the other part of the biological
fuel oil obtained in step 7) by using an oil circulating pump, then cooling the other part of the biological fuel oil by using
a biological fuel oil heat exchanger, and then conducting spray condensation with respect to the pyrolysis gas in step 7)
by using the other part of the biological fuel oil after cooling thereof; and

9) feeding one part of the non-condensable pyrolysis gas obtained in step 8) to a combustion bed to combust with air, and
conveying the other part of the non-condensable pyrolysis gas obtained in step 7) to the pyrolysis bed as a fluidizing medium.

US Pat. No. 9,157,420

DISH-TYPE STIRLING SOLAR GENERATOR

Wuhan Kaidi Engineering T...

1. A Stirling solar generator dish, comprising:
a Stirling solar generating dish set (1) comprising a combustor (2), a position adjustment mechanism (3), and a bracket (1a), the combustor (2) comprising an opening;

a fuel supply system (4) of the combustor (2) connected to the combustor (2) via a main switch valve (4c), a branch switch valve (5), a regulating valve (6), and a flexible conveying pipe (7);

the position adjustment mechanism (3) adjusting the opening of the combustor (2) to align or deviate from a heat receiver of the Stirling solar generating dish set (1);

the position adjustment mechanism (3) being disposed on the bracket (1a) of the Stirling solar generating dish set (1); and

the combustor (2) being disposed on the position adjustment mechanism (3).

US Pat. No. 9,290,383

METHOD FOR RECYCLING EXHAUST GASES FROM FISCHER-TROPSCH SYNTHESIS

Wuhan Kaidi Engineering T...

1. A method for recycling exhaust gas from Fischer-Tropsch synthesis, the method comprising:
1) introducing raw gas obtained from gasification of coal or biomass to a shift reactor, the raw gas comprising hydrogen and
carbon monoxide, conducting a water-gas shift reaction in the presence of a catalyst and, in the presence of water vapor,
transforming a part of the carbon monoxide in the raw gas to carbon dioxide and hydrogen, removing carbon dioxide produced
from the water-gas shift reaction, and collecting syngas; wherein: a molar ratio of hydrogen to carbon monoxide in the raw
gas is between 0.1 and 2.2; the syngas comprises more than 50% (v/v) of hydrogen and carbon monoxide, and a molar ratio of
hydrogen to carbon monoxide in the syngas is between 1.6 and 3.0;

2) introducing the syngas to a Fischer-Tropsch reactor for Fischer-Tropsch synthesis, whereby yielding a hydrocarbon fuel
and exhaust gas, returning part of the exhaust gas as recycle gas and mixing the recycle gas with the syngas to obtain a first
gas mixture, and introducing the first gas mixture to the Fischer-Tropsch reactor;

3) introducing the remainder of the exhaust gas to a methanation reactor, allowing hydrocarbons having two or more carbon
atoms in remainder of the exhaust gas and water vapor to react via a methanation reaction to produce methane, and obtaining
a second gas mixture comprising methane;

4) introducing the second gas mixture to a methane reforming reactor, allowing methane in the second gas mixture and water
vapor to react via a methane reforming reaction in the presence of a reforming catalyst, to yield hydrogen and carbon monoxide,
and obtaining a third gas mixture comprising hydrogen and carbon monoxide;

5) transporting the third gas mixture from the methane reforming reactor to a gas separator, separating hydrogen from the
third gas mixture, and obtaining a fourth gas mixture comprising carbon monoxide and inert components;

6) introducing a first part of the hydrogen obtained in step 5) to the Fischer-Tropsch reactor; and
7) returning the fourth gas mixture comprising carbon monoxide and the inert components to the methane reforming reactor as
a supplementary fuel to supply to supply heat energy.

US Pat. No. 9,127,022

METHOD FOR PREPARING SURFACE-MODIFIED NANOSILICON DIOXIDE FROM RICE HULLS

Wuhan Kaidi Engineering T...

1. A method for preparing surface-modified nano silicon dioxide from rice hulls, the method comprising:
1) pretreating rice hulls using a treating gas containing CO2 to remove metal ions, impurities, and dusts, and desiccating and grinding the rice hulls;

2) submerging the rice hulls into a dilute solution of a solute selected from the group consisting of phosphoric acid, boric
acid, hydrochloric acid, formic acid, acetic acid, propionic acid, butyric acid, or a strong-acid-weak-base salt for between
4 and 8 hrs, controlling an immersion temperature not to exceed 10° C., leaching a resulting mixture, removing a filtrate,
and desiccating the rice hulls; and

3) calcining the rice hulls in the absence of oxygen at a temperature of between 300 and 450° C., whereby obtaining a surface-modified
nano silicon dioxide.

US Pat. No. 9,527,783

CATALYST FOR METHANATION OF CARBON DIOXIDE, PREPARATION METHOD AND USAGE THEREOF

WUHAN KAIDI ENGINEERING T...

1. A method for preparing a catalyst for methanation of carbon dioxide, the method comprising:
1) preparing an aqueous solution comprising between 5 and 30 wt. % of a nickel compound;
2) calcining ash from the biomass power plant at a temperature of between 300 and 400° C. for between 20 and 40 min for removing
combustible impurities from the ash to obtain a second ash, wherein the ash from the biomass power plant and the second ash
comprise SiO2, Al2O3, CaO, Fe2O3, TiO2, MgO, and K2O;

3) mixing the aqueous solution obtained in 1) with the second ash obtained in 2), and stirring a resulting mixture for between
5 and 10 h for uniformly impregnating the mixture;

4) desiccating the mixture obtained in 3) at a temperature of between 110 and 150° C. for between 0.5 and 1.5 h; and
5) calcining the mixture obtained in 4) at a temperature of between 400 and 500° C. for between 3 and 6 h to yield the catalyst.

US Pat. No. 10,072,530

HYBRID POWER GENERATION SYSTEM USING SOLAR ENERGY AND BIOENERGY

WUHAN KAIDI ENGINEERING T...

1. A hybrid power generation system, comprising:a solar thermal boiler system, the solar thermal boiler system comprising a trough solar collector, a heat collector, an oil circulating pump, a storage tank for storing heat transfer oil, a solar thermal heater, a solar thermal evaporator, a main pipe transporting saturated steam, an auxiliary boiler, and a first flow distributor;
a biomass boiler system; and
a turbogenerator system, the turbogenerator system comprising a turbine, a generator, a condenser, a condensate pump, a first heater, a deaerator, a feed water pump, and a second heater;
wherein:
the trough solar collector is integrated with the heat collector to form a unit, and a plurality of units are connected in parallel or in series to form a solar light field for collecting solar energy and transforming the solar energy into heat carried by the heat transfer oil;
the solar light field is connected to the solar thermal evaporator and the solar thermal heater;
the oil circulating pump is adapted to pump the heat transfer oil in the storage tank to the solar light field;
the solar thermal evaporator is adapted to generate a solar thermal steam by the heat carried by the heat transfer oil;
the auxiliary boiler is parallel to the solar thermal evaporator and the solar thermal heater, and is adapted to generate an auxiliary steam by utilizing heat transformed from an auxiliary heat source instead of the solar energy;
the auxiliary boiler and the solar thermal evaporator are connected to the main pipe, and the main pipe is adapted to mix the solar thermal steam and the auxiliary steam respectively generated by the solar thermal evaporator and the auxiliary boiler into a mixed steam;
a flow of the mixed steam is constant, and a flow ratio of the solar thermal steam to the auxiliary steam is adjustable;
the first flow distributor is connected to the main pipe via the solar thermal heater, the solar thermal evaporator, and the auxiliary boiler;
the first flow distributor is adapted to adjust the flow ratio of the solar thermal steam to the auxiliary steam according to an intensity of the solar energy;
the main pipe is connected to the biomass boiler system; the biomass boiler system is adapted to produce a biomass steam, and superheat the mixed steam output from the solar thermal boiler system and the biomass steam into a superheated steam;
a flow of the biomass steam is constant;
the turbine is connected to the biomass boiler system for receiving the superheated steam, and the generator is connected to the turbine; the superheated steam expands in the turbine and drives the generator to generate electricity;
the turbine is connected to the condenser; the condenser is adapted to condense waste steam of the turbine to be a condensate;
the condensate is pressurized by the condensate pump, and the condensate pump is connected to the first heater; the first heater is adapted to heat the condensate, and the first heater is connected to the deaerator to produce a feed water; the feed water output from the deaerator is pumped to the second heater via the feed water pump; the second heater is adapted to heat the feed water; and
when in use, the heat transfer oil output from the solar light field of the solar thermal boiler system is transmitted through and transfers heat to the solar thermal evaporator and the solar thermal heater, and the heat transfer oil returns to the storage tank; the heat transfer oil in the storage tank is pumped to the solar light field via the oil circulating pump; the solar thermal steam generated at the solar thermal evaporator is transmitted through the main pipe transporting saturated steam to the biomass boiler system; the auxiliary steam is transmitted through the main pipe in which the auxiliary steam is mixed with the solar thermal steam generated at the solar thermal evaporator to the biomass boiler system; the mixed steam and the biomass steam generated by the biomass boiler system are superheated to 540° C.±5° C. in the biomass boiler system; and the superheated steam is transmitted to the turbine and expands in the turbine to drive the generator to generate electricity.

US Pat. No. 9,410,095

METHOD OF GASIFICATION OF BIOMASS USING GASIFICATION ISLAND

WUHAN KAIDI ENGINEERING T...

1. A method of gasification of biomass using a gasification island, the gasification island comprising: a biomass pre-treatment
and storage unit, a biomass feeder, an external heat source, a gasifier, a crude syngas cooling unit, a crude syngas washing
unit, a fresh syngas storage unit, and an ash and wastewater treatment unit, the method comprising:
pre-treating and storing biomass in the biomass pre-treatment and storage unit;
crushing the stored biomass in the biomass feeder;
gasifying the biomass in the gasifier by feeding the biomass to the gasifier while supplying the external heat source and
an oxidant to the gasifier, controlling an operating temperature of the gasifier at between 1300 and 1750° C., allowing the
biomass to fully contact with the oxidant so that desiccation, volatile matter precipitation, pyrolysis, and gasification
reaction occur, respectively, whereby yielding a crude syngas and an ash;

removing a slag from the gasifier in a liquid state;
cooling the crude syngas by introducing the crude syngas to a quench tower and a two-stage waste heat boiler of the cooling
unit to decrease the temperature of the crude syngas to between 85 and 200° C. and to recover the sensible heat; and

washing the crude syngas after sensible heat recovery in the washing unit and removing the dust therefrom in an electric dust
precipitator of the ash and wastewater treatment unit to obtain the clean and fresh syngas having both a dust content and
a tar content of 10 mg/Nm3 and a temperature of 45° C.;

transporting the clean and fresh syngas to the gas storage tank for storage;wherein
the gasification island is operated at a negative pressure.

US Pat. No. 9,151,277

METHOD AND SYSTEM FOR POWER GENERATION

Wuhan Kaidi Engineering T...

1. A method of power generation, comprising the following steps:
1) igniting a biomass boiler comprising a boiler drum when a water level of the boiler drum reaches a preset water level;
and starting a turbonator unit according to an operating procedure of a biomass boiler power plant;

2) starting a solar concentrating collector; measuring a water temperature t3 at a water outlet main of the solar concentrating collector; opening a second control valve arranged between the water outlet
main and the boiler drum when t3 ?95° C., and opening a third control valve to supply water to a solar collector tube; introducing the water into the boiler
drum; adjusting the water supply to the solar collector tube to maintain t3?95° C.; and maintaining the water level of the boiler drum, a vapor pressure, and a vapor temperature at a vapor outlet of
the biomass boiler at rated values and maintaining a steady operation of the turbonator unit by self-regulating of a control
system of the turbonator unit;

3) closing the second control valve of the water outlet main and the third control valve to prevent water in the solar collector
tube from running and to maintain the water in a heat preserving and inactive state if the water supply to the solar collector
tube is adjusted to a lowest value while the water temperature t3 at the water outlet main of the solar concentrating collector detected by the turbonator unit decreases and t3<95° C.; turning the turbonator unit into a thermal power generation mode; increasing a fuel input into the biomass boiler
by self-regulating of the control system of the turbonator unit to maintain the vapor pressure and the vapor temperature at
the vapor outlet of the biomass boiler at rated values and to maintain the steady operation of the turbonator unit;

4) opening a first control valve arranged between the water outlet main of the solar concentrating collector and a water supply
tank if the water temperature t3 at the water outlet main of the solar concentrating collector continues decreasing and when t3=5-9° C.; opening a bleed valve to drain room temperature water from the solar collector tube into a desalting water tank;
opening a drain valve to remove remaining water from pipes; introducing compressed air via an opening of an exhaust valve
into all pipes until no water remains; maintaining the solar concentrating collector and pipes at an anhydrous and antifreezing
state; and turning the turbonator unit into a biomass boiler power generation mode; and

5) repeating step 1) if the water temperature in the solar collector tube increases and t3?95° C. due to a recovery of a solar radiation; supplying water to the biomass boiler; and decreasing the fuel input into
the biomass boiler by self-regulating of the turbonator unit.

US Pat. No. 9,266,097

COBALT-BASED NANO CATALYST AND PREPARATION METHOD THEREOF

Wuhan Kaidi Engineering T...

1. A catalyst, comprising a metal combination as a core and a porous material as a shell, wherein
the metal combination comprises: a first metal component being Co, a second metal component being selected from Ce, La, and
Zr, and a third metal component being selected from Pt, Ru, Rh, and Re;

the catalyst comprises: between 10 and 35 wt. % of the first metal component, between 0.5 and 10 wt. % of the second metal
component, between 0.02 and 2 wt. % of the third metal component, and the remainder being the porous material functioning
as a carrier;

the porous material is a nano silica or alumina;
the carrier is in the shape of a spheroid, and has a pore size of between 1 and 20 nm and a specific area of between 300 and
500 m2/g; and

the metal combination has a particle size of between 0.5 and 20 nm.
US Pat. No. 10,005,966

METHOD FOR MODIFYING BIO-OIL DERIVED FROM BIOMASS PYROLYSIS

WUHAN KAIDI ENGINEERING T...

1. A method for modifying bio-oil produced from biomass pyrolysis, the method comprising:1) adding an inorganic salt and an organic demulsifier to a bio-oil, a mass ratio of the inorganic salt to the bio-oil being between 1:2000 and 1:800, and a mass ratio of the organic demulsifier and the bio-oil being between 1:4000 and 1:1000; oscillating or stirring a resulting mixture, resting the resulting mixture, to yield a lower layer being an aqueous solution and an upper layer being the bio-oil, and collecting the bio-oil, wherein the inorganic salt comprises at least one of the following ions: Na+, K+, NH4+, and NO3?;
2) employing a zeolite molecular sieve-loaded clay as a catalyst, and aging the catalyst at a temperature of between 500 and 800° C. for between 2 and 8 hours using steam, to yield a modified catalyst; and
3) adding the modified catalyst obtained in 2) to a conventional catalytic cracking reactor, injecting the bio-oil obtained in 1) to the conventional catalytic cracking reactor using a piston pump, a ratio of the catalyst to the bio-oil being between 3 and 16, and allowing the bio-oil to react under a weight hourly space velocity (WHSV) of between 6 and 15 h?1, a temperature of between 380 and 700° C., and a pressure between 0.1 and 0.8 megapascal.

US Pat. No. 9,873,841

ENTRAINED-FLOW GASIFIER AND GASIFICATION METHOD USING THE SAME FOR SYNTHESIZING SYNGAS FROM BIOMASS FUEL

WUHAN KAIDI ENGINEERING T...

1. A method for gasifying biomass using a gasifier, the gasifier comprising
a furnace body comprising a fuel inlet, a syngas outlet and a slag outlet, the fuel inlet comprising nozzles; and
a fuel pretreatment system comprising a feeding hopper;
wherein:
the furnace body is vertically disposed;
the fuel inlet is disposed at a lower part of the furnace body;
the syngas outlet is disposed at a top of the furnace body;
the slag outlet is disposed at a bottom of the furnace body;
the fuel pretreatment system is disposed outside of the furnace body;
a bottom of the feeding hopper is connected to the furnace body via the nozzles;
the nozzles are disposed radially along the furnace body; and
one or two layers of microwave plasma generators are disposed in parallel at a gasification zone of the furnace body and each
layer of the microwave plasma generators comprises working gas inlets;

the method comprising:
1) crushing and sieving a biomass fuel using the fuel pretreatment system to yield particle size-qualified fuel particles,
and transporting the particle size-qualified fuel particles to the feeding hopper;

2) introducing working gas from the working gas inlets into the microwave plasma generator, exciting the working gas to yield
high temperature, high degree of ionization, and high activity of plasma, and spraying the plasma to into the gasifier;

3) spraying the particle size-qualified fuel particles into the gasifier via the nozzles, synchronously spraying an oxidizer
via an oxygen/vapor inlet into the gasifier, so that a thermal-chemical reaction between the fuel particles and the oxidizer
in the presence of high activity of plasma proceeds to yield syngas comprising carbon monoxide and hydrogen; and

4) monitoring the temperature and components of the syngas, regulating oxygen flow rate, vapor flow rate, and microwave power
to maintain the process parameters within a preset range, collecting the syngas having a temperature of between 900 and 1200°
C. from the syngas outlet at the top of the furnace body, and discharging liquid slags from the slag outlet.

US Pat. No. 9,234,082

POLYMER MATERIAL HAVING HIGH CAPACITY FOR HYDROGEN STORAGE AND PREPARATION METHOD THEREOF

Wuhan Kaidi Engineering T...

1. A hydrogen storage material prepared by: (1) aminating a side chain or a terminal group of a linear polymer using a polyamine
compound to yield an aminated polymer and (2) reacting the aminated polymer with borohydride to yield a polymer product comprising
an ammonia borane derivative grafted to the side chain or the terminal group of the linear polymer.

US Pat. No. 10,131,855

METHOD AND DEVICE FOR PYROLYSIS OF BIOMASS TO PRODUCE SYNGAS

WUHAN KAIDI ENGINEERING T...

1. A method for pressurized pyrolysis of biomass in a pressurized pyrolysis furnace, the method comprising:1) crushing and screening biomass; collecting biomass having desired particle sizes; and delivering the biomass having desired particle sizes to a pulse-type feeding system;
2) transporting the biomass to a pyrolysis furnace via the pulse-type feeding system in a dense-phase static pressure mode in the presence of seal air; synchronously initiating microwave and a plasma torch, the microwave producing a microwave field in the pyrolysis furnace, working gas of the plasma torch being initially ionized to produce plasma jet entering the pyrolysis furnace;
in the pyrolysis furnace, biomass particles absorbing microwave and being heated from outside to inside instantaneously, and then being activated; under the action of rising syngas and microwave energy, the biomass particles being dried instantaneously and pyrolyzed to yield syngas, small amount of ash residue and coke, the ash residue and the coke constituting a fixed bed layer moving down;
under the electromagnetic coupling of the microwave field, the plasma jet constantly ionizing gas around charged ions to form a secondary ionic field, thus accelerating the heat and mass transfer efficiency of the biomass particles; at the bottom of the fixed bed layer, the plasma jet completely converting the coke or other carbonaceous materials into syngas;
with the fixed bed layer moving down, rising syngas heating the fixed bed layer and providing carbon dioxide as raw material gas for pyrolysis, and ash residue free of carbon continuing moving down; the ash residue containing free of carbon being in a liquid state and accumulating at the bottom of the pyrolysis furnace, discharging accumulated liquid ash residue regularly or continuously to maintain a preset slag level; and
3) allowing the syngas generated in 2) to continue moving upwards and introducing the syngas out from the top of the pyrolysis furnace; chilling the syngas using circulating syngas in a pipe; introducing the syngas to a cyclone separator to separate residues; and then cooling and purifying the syngas using a cooling device and a purifying device, respectively, to produce clean syngas.

US Pat. No. 9,841,008

SOLAR AND STEAM HYBRID POWER GENERATION SYSTEM

WUHAN KAIDI ENGINEERING T...

1. A solar and external steam hybrid power generation system, comprising:
a) a solar steam generator for generating a steam by using solar energy;
b) an external steam regulator, the external steam regulator comprising a heat exchanger;
c) a turboset;
d) a power generator, the power generator being coupled to the turboset;
e) a condenser;
f) a deaerator;
g) a water feed pump;
h) a first regulating valve;
i) a second regulating valve;
j) a first switch valve;
k) a second switch valve;
l) a third switch valve;
m) a fourth switch valve; and
n) a water-return bypass;wherein:
a steam outlet end of the solar steam generator is connected to a steam inlet of the turboset via the first regulating valve
for sending the steam to the turboset;

the external steam regulator is adapted to receive an industrial waste steam and regulate a pressure and a temperature of
the industrial waste steam;

the second regulating valve is adapted to adjust a flow rate of the industrial waste steam in real-time according to an intensity
of sunlight;

a steam outlet end of the external steam regulator is also connected to the steam inlet of the turboset via the second regulating
valve and the second switch valve for sending the industrial waste steam to the turboset;

a steam outlet of the turboset is connected to an input end of the condenser, and an output end of the condenser is connected
to an input end of the deaerator;

an output end of the deaerator is connected to an input end of the water feed pump;
an output end of the water feed pump is connected to a circulating water input end of the solar steam generator via the first
switch valve; and

the output end of the water feed pump is further connected to the water-return bypass via the fourth switch valve.

US Pat. No. 9,833,760

METHOD AND DEVICE FOR PREPARING ACTIVE PARTICLE-CONTAINING STEAM

WUHAN KAIDI ENGINEERING T...

1. A method for producing an active particle-containing steam, the method comprising the following steps:
1) preparing a first steam;
2) selecting one or several non-oxidizing gases as a working gas;
3) ionizing the working gas into a plasma working medium by using a plasma generator for generating plasma; and
4) injecting the plasma working medium into a steam generator to form an ionized environment in the steam generator; wherein
the steam generator is a separate device from the plasma generator; the steam generator comprises a plasma inlet, an annular
steam inlet, an outlet, and a rotary guide vane, and the rotary guide vane is independent from the annular steam inlet and
is disposed inside the annular steam inlet; and the plasma working medium is injected into the steam generator via the plasma
inlet;

5) introducing the first steam into the steam generator via the annular steam inlet, wherein the first steam is rotated by
the rotary guide vane; and

6) allowing the first steam to contact the plasma working medium in the steam generator, wherein the first steam is heated
and activated by the plasma working medium to form the active particle-containing steam.

US Pat. No. 9,758,740

METHOD AND DEVICE FOR CONVERTING CARBON DIOXIDE IN FLUE GAS INTO NATURAL GAS

WUHAN KAIDI ENGINEERING T...

1. A device for converting carbon dioxide in flue gas into natural gas using dump energy, the device comprising:
a) a transformer and rectifier device;
b) an electrolytic cell;
c) a turbine;
d) a carbon dioxide heater;
e) a primary fixed bed reactor;
f) a secondary fixed bed reactor;
g) a natural gas condenser; and
h) a process water line;wherein
an outlet of the transformer and rectifier device is connected to a power interface of the electrolytic cell, a gas-liquid
outlet of a cathode of the electrolytic cell is connected to a gas-liquid inlet of a hydrogen separator, a liquid outlet of
the hydrogen separator is connected to a liquid reflux port of the cathode of the electrolytic cell, a H2 outlet of the hydrogen separator is connected to an inlet of a hydrogen cooler, both an outlet of the hydrogen cooler and
an outlet of the carbon dioxide heater are connected to an inlet of the primary fixed bed reactor;

an outlet of the primary fixed bed reactor is connected to an inlet of the secondary fixed bed reactor successively through
a superheater and a mixed gas line of a primary heat exchanger, and an outlet of the secondary fixed bed reactor is connected
to an inlet of the natural gas condenser successively through a secondary heat exchanger and a mixed gas line of a preheater;
and

the process water line is connected to an aqueous medium inlet of the preheater, an aqueous medium outlet of the preheater
is connected to a steam inlet of the superheater through a steam pocket, a steam outlet of the superheater is connected to
a steam inlet of the turbine, and an electric outlet of the turbine is connected to an inlet of the transformer and rectifier
device.

US Pat. No. 9,758,844

METHOD FOR RECOVERING RUTHENIUM FROM SPENT RUTHENIUM-BASED CATALYST CARRIED ON ALUMINUM OXIDE

WUHAN KAIDI ENGINEERING T...

1. A method for recovering ruthenium from a spent ruthenium-based catalyst carried on aluminum oxide, the method comprising:
1) drying a spent ruthenium-based catalyst carried on aluminum oxide at 100-150° C. in a nitrogen atmosphere for 1-2 hours,
calcining the spent ruthenium-based catalyst carried on aluminum oxide at 300-500° C. for 2-4 hours, cooling the spent ruthenium-based
catalyst carried on aluminum oxide to room temperature, and grinding the spent ruthenium-based catalyst carried on aluminum
oxide into a black powder;

2) transferring the black powder to a fluidized bed reactor, purging the fluidized bed reactor with nitrogen for 20-40 minutes
and then purging the fluidized bed reactor with hydrogen, and heating the black powder in a hydrogen atmosphere at a temperature
of 200-400° C. and a pressure of 1-2 MPa for 2-3 hours to obtain a powder comprising ruthenium;

3) purging the fluidized bed reactor with nitrogen for 20-40 minutes, and then heating the powder comprising ruthenium in
a mixed atmosphere of oxygen and ozone at a temperature of 500-750° C. and a pressure of 1-2 MPa for 1-8 hours to obtain a
RuO4 gas;

4) absorbing the RuO4 gas with 3-8 mol/L hydrochloric acid to obtain a H3RuCl6 solution;

5) adding an excess oxidant to the H3RuCl6 solution, stirring the H3RuCl6 solution for 0.5-1.5 hours to completely oxidize H3RuCl6 into H2RuCl6 to obtain a H2RuCl6 solution, adding excess NH4Cl to the H2RuCl6 solution and stirring at 60-90° C. for 1-3 hours to obtain a mixture, filtering the mixture to obtain a filter cake, and washing
the filter cake to obtain solid (NH4)2RuCl6, wherein the oxidant is a soluble chlorate; and

6) reducing the solid (NH4)2RuCl6 at a temperature of 450-800° C. in a mixed atmosphere of hydrogen and nitrogen to obtain ruthenium, wherein a volume fraction
of hydrogen in the mixed atmosphere of hydrogen and nitrogen is 1-15%.

US Pat. No. 9,909,496

POWER GENERATION SYSTEM

WUHAN KAIDI ENGINEERING T...

1. A power generation system, the system comprising:
a) a solar energy concentration system;
b) a biomass gasification device;
c) a gas-powered generator;
d) a steam turbine, the steam turbine comprising a first cylinder, a second cylinder, and a third cylinder; pressures of the
first cylinder, the second cylinder, and the third cylinder respectively decreasing;

e) a steam-powered generator;
f) a solar energy heat exchange system, the solar energy heat exchange system comprising a steam outlet;
g) a first compressor;
h) a combustion chamber;
i) a gas turbine, the gas turbine comprising a gas outlet;
j) a gas exhaust heat system, the gas exhaust heat system comprising a first steam outlet and a second steam outlet, and a
pressure of the first steam outlet being higher than a pressure of the second steam outlet; and

k) a steam mixing regulating system, the steam mixing regulating system comprising a mixed steam outlet;wherein
the solar energy concentration system is connected to the solar energy heat exchange system; the biomass gasification device
is connected to the gas-powered generator via the first gas compressor, the combustion chamber, and the gas turbine; the gas
outlet of the gas turbine is connected to the gas exhaust heat system; the second steam outlet of the gas exhaust heat system
is connected to the second and the third cylinders of the steam turbine; the first steam outlet of the gas exhaust heat system
and the steam outlet of the solar energy heat exchange system are connected to the steam mixing regulating system; and the
mixed steam outlet of the steam mixing regulating system is connected to the first cylinder of the steam turbine.

US Pat. No. 9,518,235

ENTRAINED-FLOW GASIFIER AND GASIFICATION METHOD USING THE SAME FOR SYNTHESIZING SYNGAS FROM BIOMASS FUEL

WUHAN KAIDI ENGINEERING T...

1. A gasifier, comprising: a furnace body and a fuel pretreatment system, wherein the furnace body is vertically disposed
and comprises a fuel inlet disposed at a lower part of the furnace body, a syngas outlet disposed at a top of the furnace
body, and a slag outlet disposed at a bottom of the furnace body;
the fuel inlet comprises nozzles;
the fuel pretreatment system is disposed outside of the furnace body, and comprises a fuel crushing apparatus, a sieving apparatus
disposed downstream to the fuel crushing apparatus, a first fuel container for receiving particle size-qualified fuel, a second
fuel container for receiving particle size-unqualified fuel, and a feeding hopper disposed downstream to the first fuel container;

the first fuel container and the second fuel container are disposed side-by-side downstream to the sieving apparatus;
a bottom of the feeding hopper is connected to the furnace body via the nozzles;
a monitoring unit is disposed close to the syngas outlet at the top of the furnace body;
the nozzles are disposed radially along the furnace body and are between 2 and 4 in number; and
one or two layers of microwave plasma generators are disposed in parallel at a gasification zone of the furnace body, and
each layer of the microwave plasma generator comprises between 2 and 4 working gas inlets.

US Pat. No. 10,227,537

METHOD OF HYDROTREATMENT OF FISCHER-TROPSCH SYNTHESIS PRODUCTS

WUHAN KAIDI ENGINEERING T...

1. A method of hydrotreatment of Fischer-Tropsch synthesis products, the method comprising:1) mixing Fischer-Tropsch wax with a sulfur-containing liquid additive, contacting a resulting mixture with hydrogen, feeding a hydrogen-containing mixture to a first reaction region comprising a hydrogenation pretreatment catalyst, feeding an effluent from the first reaction region to a second reaction region comprising a hydrocracking catalyst, and carrying out hydrocracking reaction;
2) feeding a hydrocracking product from the second reaction region and Fischer-Tropsch naphtha and diesel fuel to a third reaction region comprising a hydrofining catalyst, carrying out hydrofining reaction; feeding an effluent from the hydrofining reaction to a fourth reaction region comprising a hydroisomerizing pour-point depressant catalyst, and carrying out hydroisomerizing pour-point depression reaction; and
3) feeding an effluent from the fourth reaction region to a gas-liquid separation system C to yield hydrogen-rich gas and liquid products, recycling the hydrogen-rich gas, feeding the liquid products to a distilling system D, to yield naphtha, diesel fuel and tail oil, and returning the tail oil to the second reaction region.
US Pat. No. 10,189,013

MONOLITHIC CATALYST COMPRISING MOLECULAR SIEVE MEMBRANE AND METHOD FOR PREPARING THE MONOLITHIC CATALYST

WUHAN KAIDI ENGINEERING T...

1. A method for preparing a monolithic catalyst comprising:cobalt;
a matrix, the matrix comprising at least one metal selected from the group consisting of silver, gold, copper, platinum, titanium, molybdenum, iron, and tin;
an additive, the additive being lanthanum, zirconium, cerium, rhodium, platinum, rhenium, ruthenium, titanium, magnesium, calcium, strontium, or a mixture thereof; and
a molecular sieve membrane, the molecular sieve membrane being mesoporous silica SBA-16 which is disposed on a surface of the metal matrix and is a carrier of the cobalt and the additive;
wherein
a thickness of the carrier of the molecular sieve membrane is between 26 and 67 ?m, the method comprising:
1) washing a plurality of metal matrixes having a honeycomb-shape and uniform sizes using deionized water; and drying the metal matrixes in an oven at 100° C.;
2) dissolving molecular sieve powders of the mesoporous silica SBA-16 in absolute ethanol to yield a mixture; oscillating the mixture for 20 to 30 min using an ultrasonic oscillation method to form a uniformly distributed soak solution of the molecular sieve powders; soaking the metal matrixes pretreated in 1) in the soak solution for 1 to 10 s; taking the metal matrixes out, and when the soak solution on the metal matrixes stops flowing and dripping down, soaking the metal matrixes in the soak solution again; repeating the impregnation of the metal matrixes, and then drying the metal matrixes in air;
3) placing the metal matrixes obtained in 2) in a molecular sieve solution of mesoporous silica SBA-16 and crystallizing the mesoporous silica SBA-16 for 5 to 120 hrs at a temperature of between 70 and 150° C. in a reaction still; allowing the mesoporous silica SBA-16 to grow in-situ on a surface of the metal matrixes to yield metal matrixes comprising a molecular sieve membrane; taking out the metal matrixes comprising the molecular sieve membrane, washing the metal matrixes comprising the molecular sieve membrane using deionized water, and drying; and roasting the metal matrixes comprising the molecular sieve membrane for 4 to 8 hrs at a temperature of between 400 and 600° C.; and
4) soaking the metal matrixes comprising the molecular sieve membrane obtained in 3) in a solution of a cobalt salt and the additive for 1 to 20 min; drying the metal matrixes comprising the molecular sieve membrane and aging at room temperature for 3 to 36 hrs; roasting the metal matrixes comprising the molecular sieve membrane for 6 to 12 hrs at a programmed temperature of between 300 and 550° C., and then gradually cooling the metal matrixes comprising the molecular sieve membrane to room temperature.

US Pat. No. 9,902,907

SYSTEM FOR PRODUCING SYNTHESIS GAS FROM BIOMASS

WUHAN KAIDI ENGINEERING T...

1. A gasification system for producing synthesis gas from biomass, the system comprising:
a biomass material pre-processing part, the biomass material pre-processing part comprising a crushing system, a drying system,
and a biomass stock bin;

a pyrolysis part, the pyrolysis part comprising a pyrolysis bed, a carrier heating fluidized bed, and a separating system;
a combustion bed;
a condensing part, the condensing part comprising a condensate tank, an oil circulating pump, and a fuel oil heat exchanger;
the condensate tank comprising a first portion and a second portion;

a non-condensable pyrolysis gas compressor;
a waste gas pipe; and
a gasification part, the gasification part comprising a fuel oil tank and a gasification furnace;wherein
the crushing system is connected to the drying system;
the drying system is connected to the biomass stock bin;
the biomass stock bin is connected to the pyrolysis bed via a first pipe;
the pyrolysis bed is connected to the separating system;
the separating system is connected to the carrier heating fluidized bed;
the carrier heating fluidized bed is connected to the drying system through the waste gas pipe;
the combustion bed is connected to the carrier heating fluidized bed;
the separating system is connected to the first portion;
the first portion is connected to the second portion;
the second portion is connected to the oil circulating pump;
the oil circulating pump is connected to the fuel oil heat exchanger;
the fuel oil heat exchanger is connected to the first portion;
the second portion is connected to the non-condensable pyrolysis gas compressor;
the second portion is connected to the fuel oil tank;
the fuel oil tank is connected to the gasification furnace via a second pipe; and
an output of the non-condensable pyrolysis gas compressor is connected to the pyrolysis bed and the combustion bed.
US Pat. No. 9,795,950

CATALYST FOR PREPARING AVIATION FUEL FROM FISCHER-TROPSCH PRODUCTS AND METHOD FOR PREPARING SAID CATALYST

WUHAN KAIDI ENGINEERING T...

1. A catalyst, comprising:
between 20 and 50 percent by weight of an amorphous aluminum silicate;
between 5 and 20 percent by weight of alumina;
between 20 and 60 percent by weight of a hydrothermally modified zeolite;
between 0.5 and 1.0 percent by weight of a Sesbania powder;
between 0.5 and 5 percent by weight of nickel oxide; and
between 5 and 15 percent by weight of molybdenum oxide.
US Pat. No. 10,286,389

CARRIER AND CATALYST FOR SELECTIVELY SYNTHESIZING KEROSENE FRACTION FROM SYNGAS, AND METHOD FOR PREPARING THE SAME

WUHAN KAIDI ENGINEERING T...

1. A carrier, comprising the following components in parts by weight: 5-50 parts of mesoporous zirconia (ZrO2), 10-55 parts of a silicoaluminophosphate (SAPO) molecular sieve, 5-50 parts of modified mesoporous molecular sieve Al-SBA-16, 1-3 parts of sesbania gum powder, and 10-70 parts of alumina.

US Pat. No. 10,266,776

IRON-BASED CATALYST, METHOD FOR PREPARING THE SAME, AND METHOD FOR PRODUCING ALPHA-OLEFINS USING THE SAME

WUHAN KAIDI ENGINEERING T...

1. A method for preparing a catalyst, the method comprising:1) mixing anhydrous ferric nitrate, a nitrate of a first additive, and amorphous silicon dioxide with n-octanol to form a first solution, wherein a total weight percentage of the anhydrous ferric nitrate, the nitrate of the first additive, and the amorphous silicon dioxide in the first solution is between 3 wt. % and 20 wt. %; stirring and heating the first solution to a temperature of between 140 and 180° C. for 4 hrs to yield a heated first solution; cooling and filtering the heated first solution to yield a first product; drying the first product to yield a black solid; grinding the black solid for 20 to 40 mins to yield a ground black solid, then roasting the ground black solid for 5 hrs at between 400 and 600° C. to yield a catalyst precursor; and
2) dissolving a precursor of a second additive in water or ethyl alcohol to form a second solution; performing dry impregnation by adding the second solution to the catalyst precursor to yield an impregnated catalyst precursor; conducting an aging treatment of the impregnated catalyst precursor for between 12 and 24 hrs to form a second product; drying the second product at a temperature of between 100 and 130° C. to yield a dried second product, and roasting the dried second product for 4 to 10 hrs at a temperature of between 300 and 1200° C. to yield a roasted second product; and tableting and sieving the roasted second product to yield the catalyst;wherein:the catalyst comprises, by a total weight of the catalyst, between 50.0 and 99.8 percent by weight of iron, between 0 and 5.0 percent by weight of the first additive, between 0 and 10 percent by weight of the second additive, and a carrier;
the first additive is ruthenium, platinum, copper, cobalt, or zinc, or the first additive is a metal oxide selected from oxides of ruthenium, platinum, copper, cobalt, and zinc;
the second additive is lanthanum oxide, cerium oxide, magnesium oxide, aluminum oxide, potassium oxide, manganese oxide, or zirconium oxide; and
the carrier is silicon dioxide.

US Pat. No. 10,363,550

MESOPOROUS MATERIAL-COATED COBALT-BASED CATALYST FOR FISCHER-TROPSCH SYNTHESIS AND METHOD FOR PREPARING THE SAME

WUHAN KAIDI ENGINEERING T...

1. A catalyst, comprising:elemental cobalt;
a carrier, the carrier comprising silica; and
a selective promoter, the selective promoter comprising zirconium; wherein:
the elemental cobalt and the selective promoter are disposed on a surface of the carrier;
outer surfaces of the elemental cobalt and the selective promoter are coated with a shell layer comprising a mesoporous material; and
a hydrophobic organic compound is disposed on an exterior surface of the shell layer.

US Pat. No. 10,370,602

APPARATUS AND METHOD FOR PRODUCING DIESEL FUEL AND JET FUEL USING FISCHER-TROPSCH SYNTHETIC OIL

WUHAN KAIDI ENGINEERING T...

2. A method for producing diesel fuel and jet fuel, the method comprising:1) transporting Fischer-Tropsch synthetic oil to a pipe that is connected to a raw material inlet of a hydrofining reactor through an oil mixture inlet pipe, introducing circulating hydrogen to the pipe through a circulating hydrogen inlet pipe, mixing and inputting the circulating hydrogen and the Fischer-Tropsch synthetic oil to the hydrofining reactor via the raw material inlet of the hydrofining reactor for a hydrofining reaction in the presence of a hydrofining catalyst to produce hydrofining products;
2) allowing the hydrofining products obtained from 1) to enter a hot separator via a hydrofining product inlet of the hot separator to produce separated oil and cracking oil gas; discharging the separated oil from the hot separator via a separated oil outlet of the hot separator and introducing the separated oil discharged from the hot separator to a first rectifying column via a separated oil inlet of the first rectifying column, discharging the cracking oil gas from the hot separator via a first gas outlet of the hot separator;
3) rectifying the separated oil to yield tail oil fraction, diesel fraction, naphtha fraction, and cracking oil gas in the first rectifying column; discharging the tail oil fraction from the first rectifying column through a tail oil fraction outlet of the first rectifying column and allowing the tail oil fraction discharged from the first rectifying column to enter a first mixing chamber through a tail oil fraction inlet of the first mixing chamber; allowing the circulating hydrogen to enter the first mixing chamber through a circulating hydrogen inlet of the first mixing chamber; mixing the tail oil fraction and the circulating hydrogen in the first mixing chamber to obtain a first resulting mixture and allowing the first resulting mixture to enter a hydrocracking reactor through a first mixture outlet of the first mixing chamber and a first mixture inlet of the hydrocracking reactor; discharging the diesel fraction from the first rectifying column through a diesel fraction outlet of the first rectifying column and allowing the diesel fraction discharged from the first rectifying column to enter a second mixing chamber through a diesel fraction inlet of the second mixing chamber; introducing renewal hydrogen to enter the second mixing chamber through a renewal hydrogen inlet of the second mixing chamber; mixing the diesel fraction and the renewal hydrogen in the second mixing chamber to obtain a second resulting mixture and allowing the second resulting mixture to enter a hydroisomerization reactor through a second mixture outlet of the second mixing chamber and a second mixture inlet of the hydroisomerization reactor; discharging the naphtha fraction from the first rectifying column through a naphtha fraction outlet of the first rectifying column; and discharging the cracking oil gas from the first rectifying column through a second gas outlet of the first rectifying column;
4) hydrocracking the first resulting mixture in the hydrocracking reactor to produce hydrocracking products; hydroisomerizing the second resulting mixture in the hydroisomerization reactor to produce hydroisomerization products;
5) discharging the hydrocracking products from the hydrocracking reactor through a hydrocracking product outlet of the hydrocracking reactor; discharging the hydroisomerization products from the hydroisomerization reactor through a hydroisomerization product outlet of the hydroisomerization reactor; mixing the hydrocracking products and the hydroisomerization products to obtain a third resulting mixture and allowing the third resulting mixture to enter a second rectifying column through a hydrogenation product mixture inlet of the second rectifying column; rectifying the third resulting mixture to produce cracking oil gas, aviation kerosene, diesel, paraffin, tail oil fraction, and naphtha fraction in the second rectifying column; discharging the aviation kerosene from the second rectifying column to an aviation kerosene tank through an aviation kerosene outlet of the second rectifying column, discharging the diesel from the second rectifying column to a diesel tank through a diesel outlet of the second rectifying column; discharging the naphtha fraction from the second rectifying column to a naphtha fraction tank through a naphtha fraction outlet of the second rectifying column;
discharging a mixture of the tail oil fraction and the paraffin from the second rectifying column through a paraffin outlet of the second rectifying column, or recycling the mixture of the tail oil fraction and the paraffin from the second rectifying column along a discharge pipe of the tail oil fraction and paraffin to enter the first mixing chamber via the tail oil fraction inlet of the first mixing chamber to mix with the circulating hydrogen and then to enter the hydrocracking reactor, wherein the paraffin outlet of the second rectifying column is connected to the discharge pipe of the tail oil fraction and paraffin via a tee joint; and discharging the cracking oil gas from the second rectifying column through a third gas outlet of the second rectifying column; and
6) mixing and introducing the cracking oil gas discharged in 2), 3), and 5) to a condensation fractionating column via the a gas inlet of the condensation fractionating column, to yield gas and liquid;
discharging the gas from the condensation fractionating column via a fourth gas outlet of the condensation fractionating column and then allowing the gas discharged from the condensation fractionating column to enter the hydrofining reactor via the pipe that is connected to the raw material inlet of the hydrofining reactor for cyclic utilization; and discharging the liquid from the condensation fractionating column via a liquid outlet of the condensation fractionating column and then converging the liquid discharged from the condensation fractionating column with the naphtha fraction discharged in 3) and 5) to yield ethylene pyrolysis materials.

US Pat. No. 10,221,360

METHOD AND DEVICE FOR FISCHER-TROPSCH SYNTHESIS

WUHAN KAIDI ENGINEERING T...

1. A method for Fischer-Tropsch synthesis, the method comprising:1) gasifying a raw material to obtain a crude syngas comprising H2, CO and CO2;
2) electrolyzing a saturated NaCl solution using a chloralkali process to obtain a NaOH solution, Cl2, and H2,
3) separating the CO2 from the crude syngas to obtain separated CO2 and a first gaseous mixture, and then absorbing the separated CO2 using the NaOH solution obtained in 2); and
4) adding the H2 obtained in 2) into the first gaseous mixture to obtain a second gaseous mixture, and then using the second gaseous mixture for Fischer-Tropsch synthesis reaction.
US Pat. No. 10,220,375

CATALYST FOR FISCHER-TROPSCH SYNTHESIS AND METHOD FOR PREPARING THE SAME, AND METHOD FOR PREPARING MODIFIED MOLECULAR SIEVE CARRIER

WUHAN KAIDI ENGINEERING T...

1. A catalyst, comprising:an active component, the active component comprising iron, manganese, copper, and potassium; and
a modified molecular sieve carrier, the modified molecular sieve carrier comprising a zeolite and a cerium salt and/or a praseodymium salt;wherein:the zeolite is SSZ-13, SAPO-34, or ZSM-5; and
the catalyst comprises between 10 and 35 wt. % of iron, between 1 and 20 wt. % of manganese, between 1 and 20 wt. % of copper, between 1 and 10 wt. % of potassium, and between 40 and 80 wt. % of the molecular sieve carrier.

US Pat. No. 10,450,519

METHOD FOR HYDROFINING OF MIDDLE DISTILLATES OF FISCHER-TROPSCH SYNTHETIC FULL-RANGE DISTILLATES

WUHAN KAIDI ENGINEERING T...

1. A method for hydrofining of middle distillates of Fischer-Tropsch synthetic full-range distillates, the method comprising:1) separating middle distillates of Fischer-Tropsch synthetic full-range distillates to yield light distillates, heavy distillates, and intermediate distillates; wherein a boiling range of the light distillates lies below 180° C.; a boiling range of the intermediate distillates is between 180° C. and 360° C.; and a boiling range of the heavy distillates lies above 360° C.;
2) metering using a metering pump the light distillates, the heavy distillates, and the intermediate distillates; providing a hydrogenation reactor filled with a hydrofining catalyst and comprising a first feed inlet, a second feed inlet, and a third feed inlet from the top down, wherein each of the first feed inlet, the second feed inlet, and the third feed inlet communicates with a hydrogen inlet, a height of the hydrogenation reactor is represented by H, the first feed inlet is disposed on a top of the hydrogenation reactor, the second feed inlet is disposed on the hydrogenation reactor at a height between ? H and ½ H as measured from the top of the hydrogenation reactor, and the third feed inlet is disposed below the second feed inlet at a height between ? H and ? H as measured from the second feed inlet; introducing the light distillates and hydrogen into the hydrogenation reactor via the first feed inlet, introducing the heavy distillates and hydrogen into the hydrogenation reactor via the second feed inlet, and introducing the intermediate distillates and hydrogen into the hydrogenation reactor via the third feed inlet; a reaction pressure in the hydrogenation reactor being between 4 MPa and 8 MPa, a ratio of the hydrogen to distillates being between 100:1 and 2000:1, a liquid hourly space velocity being between 0.1 h?1 and 5.0 h?1, and a reaction temperature being between 300° C. and 420° C.; and
3) introducing products from 2) to a gas-liquid separator to yield hydrogen and liquid products, returning the hydrogen to the hydrogenation reactor via the first feed inlet, the second feed inlet, and the third feed inlet, respectively, to mix with the light distillates, the heavy distillates, and the intermediate distillates, and introducing the liquid products to a fractionating column for further separation.